System and method for diffusion combustion with oxidant-diluent mixing in a stoichiometric exhaust gas recirculation gas turbine system

ABSTRACT

A system is provided with a turbine combustor having a first diffusion fuel nozzle, wherein the first diffusion fuel nozzle has first and second passages that separately inject respective first and second flows into a chamber of the turbine combustor to produce a diffusion flame. The first flow includes a first fuel, and the second flow includes a first oxidant and a first diluent. The system includes a turbine driven by combustion products from the diffusion flame in the turbine combustor. The system also includes an exhaust gas compressor, wherein the exhaust gas compressor is configured to compress and route an exhaust gas from the turbine to the turbine combustor along an exhaust recirculation path.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims priority to and benefit of U.S. ProvisionalPatent Application No. 61/722,118, entitled “SYSTEM AND METHOD FORDIFFUSION COMBUSTION IN A STOICHIOMETRIC EXHAUST GAS RECIRCULATION GASTURBINE SYSTEM,” filed on Nov. 2, 2012, U.S. Provisional PatentApplication No. 61/722,115, entitled “SYSTEM AND METHOD FOR DIFFUSIONCOMBUSTION WITH FUEL-DILUENT MIXING IN A STOICHIOMETRIC EXHAUST GASRECIRCULATION GAS TURBINE SYSTEM,” filed on Nov. 2, 2012, U.S.Provisional Patent Application No. 61/722,114, entitled “SYSTEM ANDMETHOD FOR DIFFUSION COMBUSTION WITH OXIDANT-DILUENT MIXING IN ASTOICHIOMETRIC EXHAUST GAS RECIRCULATION GAS TURBINE SYSTEM,” filed onNov. 2, 2012, and U.S. Provisional Patent Application No. 61/722,111,entitled “SYSTEM AND METHOD FOR LOAD CONTROL WITH DIFFUSION COMBUSTIONIN A STOICHIOMETRIC EXHAUST GAS RECIRCULATION GAS TURBINE SYSTEM,” filedon Nov. 2, 2012, all of which are herein incorporated by reference intheir entirety for all purposes.

BACKGROUND OF THE INVENTION

The subject matter disclosed herein relates to gas turbine engines.

Gas turbine engines are used in a wide variety of applications, such aspower generation, aircraft, and various machinery. Gas turbine enginegenerally combust a fuel with an oxidant (e.g., air) in a combustorsection to generate hot combustion products, which then drive one ormore turbine stages of a turbine section. In turn, the turbine sectiondrives one or more compressor stages of a compressor section, therebycompressing oxidant for intake into the combustor section along with thefuel. Again, the fuel and oxidant mix in the combustor section, and thencombust to produce the hot combustion products. Gas turbine enginesgenerally premix the fuel and oxidant along one or more flow pathsupstream from a combustion chamber of the combustor section, and thusgas turbine engines generally operate with premix flames. Unfortunately,the premix flames may be difficult to control or maintain, which canimpact various exhaust emission and power requirements. Furthermore, gasturbine engines typically consume a vast amount of air as the oxidant,and output a considerable amount of exhaust gas into the atmosphere. Inother words, the exhaust gas is typically wasted as a byproduct of thegas turbine operation.

BRIEF DESCRIPTION OF THE INVENTION

Certain embodiments commensurate in scope with the originally claimedinvention are summarized below. These embodiments are not intended tolimit the scope of the claimed invention, but rather these embodimentsare intended only to provide a brief summary of possible forms of theinvention. Indeed, the invention may encompass a variety of forms thatmay be similar to or different from the embodiments set forth below.

In a first embodiment, a system is provided with a turbine combustorhaving a first diffusion fuel nozzle, wherein the first diffusion fuelnozzle has first and second passages that separately inject respectivefirst and second flows into a chamber of the turbine combustor toproduce a diffusion flame. The first flow includes a first fuel, and thesecond flow includes a first oxidant and a first diluent. The systemincludes a turbine driven by combustion products from the diffusionflame in the turbine combustor. The system also includes an exhaust gascompressor, wherein the exhaust gas compressor is configured to compressand route an exhaust gas from the turbine to the turbine combustor alongan exhaust recirculation path.

In a second embodiment, a method includes injecting first and secondflows separately into a chamber of a turbine combustor to produce adiffusion flame, wherein the first flow includes a first fuel, and thesecond flow includes a first oxidant and a first diluent. The methodfurther includes driving a turbine with the combustion products from thediffusion flame, and outputting an exhaust gas. The method furtherincludes recirculating the exhaust gas along an exhaust recirculationpath to an exhaust gas compressor. The method further includescompressing and routing the exhaust gas to the turbine combustor.

In a third embodiment, a method includes introducing an oxidant to atleast one oxidant compressor to produce a compressed oxidant stream, andintroducing a recirculated low oxygen content gas stream to a compressorsection of a gas turbine engine to produce a compressed low oxygencontent gas stream. The method further includes mixing a first portionof the compressed low oxygen content gas stream with a first portion ofthe compressed oxidant stream and producing a diluted compressed oxidantstream. The method further includes introducing the diluted compressedoxidant stream and a fuel stream in a substantially stoichiometric ratioto at least one turbine combustor and mixing the diluted compressedoxidant stream and the fuel stream at the point of combustion andcombusting the mixture of the diluted compressed oxidant stream and thefuel stream. The method further includes introducing a second portion ofthe compressed low oxygen content gas stream to the at least one turbinecombustor and mixing it with the combusting streams of dilutedcompressed oxidant and fuel after the point of combustion and producinga high temperature high pressure low oxygen content stream. The methodfurther includes introducing the high temperature high pressure lowoxygen content stream to an expander section of the gas turbine engineand expanding the high temperature high pressure low oxygen contentstream to produce mechanical power and a recirculated low oxygen contentgas stream. The method further includes using a first portion of themechanical power to drive the compressor section of the gas turbineengine. The method further includes using a second portion of themechanical power to drive at least one of: a generator, the at least oneoxidant compressor or at least one other mechanical device. The methodfurther includes recirculating the recirculated low oxygen content gasstream in a recirculation loop from the outlet of the expander sectionto the inlet of the compressor section of the gas turbine engine. Themethod further includes extracting at least a third portion of thecompressed low oxygen content gas stream from the gas turbine engine anddelivering the at least a third portion of the compressed low oxygencontent gas stream to the first at least one oxidation catalyst unit andproducing a low oxygen content product stream.

BRIEF DESCRIPTION OF THE DRAWINGS

These and other features, aspects, and advantages of the presentinvention will become better understood when the following detaileddescription is read with reference to the accompanying drawings in whichlike characters represent like parts throughout the drawings, wherein:

FIG. 1 is a diagram of an embodiment of a system having a turbine-basedservice system coupled to a hydrocarbon production system;

FIG. 2 is a diagram of an embodiment of the system of FIG. 1, furtherillustrating a control system and a combined cycle system;

FIG. 3 is a diagram of an embodiment of the system of FIGS. 1 and 2,further illustrating details of a gas turbine engine, exhaust gas supplysystem, and exhaust gas processing system;

FIG. 4 is a flow chart of an embodiment of a process for operating thesystem of FIGS. 1-3;

FIG. 5 is a diagram of an embodiment of the exhaust gas processingsystem of FIGS. 1-3;

FIG. 6 is a diagram of an embodiment of the exhaust gas supply system ofFIGS. 1-3;

FIG. 7 is a diagram of an embodiment of the gas turbine engine of FIGS.1-3, further illustrating details of the combustor, fuel nozzle, andflows of oxidant, fuel, and diluent;

FIG. 8 is a diagram of an embodiment of the fuel nozzle of FIG. 7,illustrating a premix fuel nozzle configuration;

FIG. 9 is a diagram of an embodiment of the fuel nozzle of FIG. 7,illustrating a premix fuel nozzle configuration;

FIG. 10 is a diagram of an embodiment of the fuel nozzle of FIG. 7,illustrating a premix fuel nozzle configuration;

FIG. 11 is a diagram of an embodiment of the fuel nozzle of FIG. 7,illustrating a diffusion fuel nozzle configuration;

FIG. 12 is a diagram of an embodiment of the fuel nozzle of FIG. 7,illustrating a diffusion fuel nozzle configuration;

FIG. 13 is a diagram of an embodiment of the fuel nozzle of FIG. 7,illustrating a diffusion fuel nozzle configuration;

FIG. 14 is a schematic cross-section of an embodiment of the fuel nozzleof FIG. 13, taken along line 14-14;

FIG. 15 is a schematic cross-section of an embodiment of the fuel nozzleof FIG. 13, taken along line 14-14;

FIG. 16 is a diagram of an embodiment of the combustor and fuel nozzleof FIG. 7, illustrating a diffusion fuel nozzle configuration and adiluent injection system;

FIG. 17 is a schematic cross-section of an embodiment of the combustorand fuel nozzles of FIG. 7, taken along line 17-17, illustrating amulti-nozzle configuration of the fuel nozzles; and

FIG. 18 is a graph of gas turbine load and exhaust gas recirculation(EGR) flow versus fuel/oxidant ratio for a diffusion flame configurationand a premix flame configuration.

DETAILED DESCRIPTION OF THE INVENTION

One or more specific embodiments of the present invention will bedescribed below. In an effort to provide a concise description of theseembodiments, all features of an actual implementation may not bedescribed in the specification. It should be appreciated that in thedevelopment of any such actual implementation, as in any engineering ordesign project, numerous implementation-specific decisions must be madeto achieve the developers' specific goals, such as compliance withsystem-related and business-related constraints, which may vary from oneimplementation to another. Moreover, it should be appreciated that sucha development effort might be complex and time consuming, but wouldnevertheless be a routine undertaking of design, fabrication, andmanufacture for those of ordinary skill having the benefit of thisdisclosure.

When introducing elements of various embodiments of the presentinvention, the articles “a,” “an,” “the,” and “said” are intended tomean that there are one or more of the elements. The terms “comprising,”“including,” and “having” are intended to be inclusive and mean thatthere may be additional elements other than the listed elements.

As discussed in detail below, the disclosed embodiments relate generallyto gas turbine systems with exhaust gas recirculation (EGR), andparticularly stoichiometric operation of the gas turbine systems usingEGR. For example, the gas turbine systems may be configured torecirculate the exhaust gas along an exhaust recirculation path,stoichiometrically combust fuel and oxidant along with at least some ofthe recirculated exhaust gas, and capture the exhaust gas for use invarious target systems. The recirculation of the exhaust gas along withstoichiometric combustion may help to increase the concentration levelof carbon dioxide (CO₂) in the exhaust gas, which can then be posttreated to separate and purify the CO₂ and nitrogen (N₂) for use invarious target systems. The gas turbine systems also may employ variousexhaust gas processing (e.g., heat recovery, catalyst reactions, etc.)along the exhaust recirculation path, thereby increasing theconcentration level of CO₂, reducing concentration levels of otheremissions (e.g., carbon monoxide, nitrogen oxides, and unburnthydrocarbons), and increasing energy recovery (e.g., with heat recoveryunits). Furthermore, the gas turbine engines may be configured tocombust the fuel and oxidant with one or more diffusion flames, ratherthan or in addition to premix flames. The diffusion flames may help tomaintain stability and operation within certain limits forstoichiometric combustion, which in turn helps to increase production ofCO₂. For example, as discussed below, a gas turbine system operatingwith diffusion flames may enable a greater quantity of EGR, as comparedto a gas turbine system operating with premix flames. In turn, theincreased quantity of EGR helps to increase CO₂ production. Possibletarget systems include pipelines, storage tanks, carbon sequestrationsystems, and hydrocarbon production systems, such as enhanced oilrecovery (EOR) systems.

As general context, it is noteworthy to discuss the differences betweena premix flame (i.e., premix combustion) versus a diffusion flame (i.e.,diffusion combustion). Combustion (i.e., premix or diffusion combustion)is essentially an exothermic chemical reaction (e.g., combustionreaction) between a fuel and an oxidant, such as air, oxygen,oxygen-enriched air, oxygen reduced air, or mixtures of oxygen andnitrogen. The exothermic chemical reaction between the fuel and theoxidant may substantially impact (and control) the stability of theflame (e.g., the stability of the flame surface), and vice versa. Forexample, the heat release from the exothermic chemical reaction helps tosustain the flame, and thus higher flame temperatures generally lead togreater flame stability. In other words, higher temperatures associatedwith the exothermic chemical reaction may help to increase flamestability, whereas lower temperatures associated with the exothermicchemical reaction may reduce the flame stability. The flame temperaturemay be largely dependent on the fuel/oxidant ratio. In particular, theflame temperature may be the greatest at a stoichiometric fuel/oxidantratio, which, as discussed in detail below, generally involves anexothermic chemical reaction that consumes substantially all of the fueland oxidant, thereby resulting in substantially no residual oxidant orunburnt fuel.

With premix combustion, the fuel and oxidant mix at one or morelocations upstream from the premix flame, which is essentially acombustion of this pre-mixture of fuel and oxidant. In general, theexothermic chemical reaction of fuel and oxidant in the premix flame isconstrained to the fuel/oxidant ratio of the pre-mixture, which isachieved upstream from the premix flame. In many configurations(particularly when one or more diluents are premixed with the fuel andoxidant), it may be more difficult to maintain a substantiallystoichiometric fuel/oxidant ratio with a premix flame, and thus it maybe more difficult to maximize the stability of the flame. In certainconfigurations, the premix flame may be achieved with a fuel-leanfuel/oxidant ratio, which reduces the flame temperature and, thus, helpsto lower emissions of nitrogen oxides (NO_(X)), e.g., nitrogen monoxide(NO) and nitrogen dioxide (NO₂). While the reduced NO_(X) emissions isrelevant for emissions regulations, the reduced flame temperature alsocauses a reduction in flame stability. In the disclosed embodiments, thesystem may be controlled to provide a substantially stoichiometricfuel/oxidant ratio (e.g., increasing flame temperature and flamestability), while using one or more diluents to reduce the temperaturefor purposes of emissions control (e.g., reducing NO_(X) emissions). Inparticular, as discussed below, the diluents may be provided separatefrom the fuel and oxidant (e.g., after the point of combustion and/ordownstream from the premix flame), thereby enabling more precise controlof the fuel/oxidant ratio to achieve stoichiometric combustion whilealso using the diluents to control the temperature and emissions (e.g.,NO_(X) emissions). In other words, the fuel and oxidant flows may becontrolled independently from one another and the diluent flow, therebyproviding a more precisely controlled fuel/oxidant ratio in thepre-mixture delivered to the location of the premix flame.

With diffusion combustion, the fuel and oxidant generally do not mixupstream from the diffusion flame, but rather the fuel and oxidant mixand react directly at the flame surface and/or the flame surface existsat the location of mixing between the fuel and oxidant. In particular,the fuel and oxidant separately approach the flame surface (or diffusionboundary/interface), and then diffuse (e.g., via molecular and viscousdiffusion) along the flame surface (or diffusion boundary/interface) togenerate the diffusion flame. It is noteworthy that the fuel and oxidantmay be at a substantially stoichiometric ratio along this flame surface(or diffusion boundary/interface), which may result in a greater flametemperature (e.g., a peak flame temperature) along this flame surface.Again, the stoichiometric fuel/oxidant ratio generally results in agreater flame temperature (e.g., a peak flame temperature), as comparedwith a fuel-lean or fuel-rich fuel/oxidant ratio. As a result, thediffusion flame may be substantially more stable than the premix flame,because the diffusion of fuel and oxidant helps to maintain astoichiometric ratio (and greater temperature) along the flame surface.Although greater flame temperatures can also lead to greater exhaustemissions, such as NO_(X) emissions, the disclosed embodiments use oneor more diluents to help control the temperature and emissions whilestill avoiding any premixing of the fuel and oxidant. For example, thedisclosed embodiments may introduce one or more diluents separate fromthe fuel and oxidant (e.g., after the point of combustion and/ordownstream from the diffusion flame), thereby helping to reduce thetemperature and reduce the emissions (e.g., NO_(X) emissions) producedby the diffusion flame.

In the disclosed embodiments, the exhaust gas provided by the exhaustgas recirculation (EGR) serves as at least one of the diluents. Theexhaust gas (as one of the diluents) is essentially decoupled from theflows of oxidant and fuel, thereby enabling independent control of thefuel, oxidant, and diluent (e.g., exhaust gas) flows. In certainembodiments, the exhaust gas may be injected into the turbine combustorafter the point of combustion and/or downstream from the flame (e.g.,premix flame and/or diffusion flame), thereby helping to reduce thetemperature and reduce exhaust emissions, e.g., NO_(X) emissions.However, other diluents (e.g., steam, nitrogen, or other inert gases)also may be used for temperature and/or emissions control, alone or incombination with the exhaust gas. Given the differences between premixflames and diffusion flames, the amount of EGR may vary considerablybetween a gas turbine system operating with premix fuel nozzles versusdiffusion fuel nozzles. A premix flame may be constrained to thepre-mixture upstream from the premix flame (e.g., including mixing ofthe diluent with the fuel and oxidant), and thus, the premix flame maynot be capable of maintaining flame stability above a certain level ofEGR. In other words, in a premix flame configuration of the gas turbinesystem, an increasing amount of exhaust gas (e.g., EGR) that premixeswith the fuel and oxidant may increasingly reduce the temperature andflame stability of the premix flame, and thus too much EGR may cause thepremix flame to become unstable. However, in a diffusion flameconfiguration of the gas turbine system, it is now believed that anincreasing amount of exhaust gas (e.g., EGR) can be used along with thediffusion flame, well beyond any limits associated with a premix flameconfiguration. For example, in a substantially stoichiometric EGR gasturbine system, the amount of exhaust gas (e.g., EGR) that may be usedwith a diffusion flame configuration may be at least approximately 10,20, 30, 40, 50, 60, 70, 80, 90, or 100 percent greater than the amountof exhaust gas (e.g., EGR) that may be used with a premix flameconfiguration. By further example, in a substantially stoichiometric EGRgas turbine system, the amount of exhaust gas (e.g., EGR) that may beused with a diffusion flame configuration may be greater thanapproximately 35, 40, 45, 50, 55, 60, 65, 70, or 75 percent by volume ofthe exhaust gas (e.g., EGR) relative to the total flow through thecombustors and turbine section (e.g., total flow of oxidant, fuel, anddiluents). As a result, a significant improvement in CO₂ production maybe achieved by using diffusion flames (e.g., diffusion fuel nozzles)along with a substantially stoichiometric EGR gas turbine system.

Although the diffusion fuel nozzles may be particularly helpful inincreasing quantities of EGR and CO₂ production, the disclosedembodiments employ various controls to help control the fuel/oxidantratio, the stability of the flame, exhaust emissions, and power output,whether the system is operating with a premix flame, a diffusion flame,or a combination thereof. For example, the disclosed embodiments mayinclude combustors with one or more diffusion fuel nozzles and premixfuel nozzles, which may be independently controlled through differentfluid supply circuits to provide benefits of both premix flameconfigurations and diffusion flame configurations.

FIG. 1 is a diagram of an embodiment of a system 10 having anhydrocarbon production system 12 associated with a turbine-based servicesystem 14. As discussed in further detail below, various embodiments ofthe turbine-based service system 14 are configured to provide variousservices, such as electrical power, mechanical power, and fluids (e.g.,exhaust gas), to the hydrocarbon production system 12 to facilitate theproduction or retrieval of oil and/or gas. In the illustratedembodiment, the hydrocarbon production system 12 includes an oil/gasextraction system 16 and an enhanced oil recovery (EOR) system 18, whichare coupled to a subterranean reservoir 20 (e.g., an oil, gas, orhydrocarbon reservoir). The oil/gas extraction system 16 includes avariety of surface equipment 22, such as a Christmas tree or productiontree 24, coupled to an oil/gas well 26. Furthermore, the well 26 mayinclude one or more tubulars 28 extending through a drilled bore 30 inthe earth 32 to the subterranean reservoir 20. The tree 24 includes oneor more valves, chokes, isolation sleeves, blowout preventers, andvarious flow control devices, which regulate pressures and control flowsto and from the subterranean reservoir 20. While the tree 24 isgenerally used to control the flow of the production fluid (e.g., oil orgas) out of the subterranean reservoir 20, the EOR system 18 mayincrease the production of oil or gas by injecting one or more fluidsinto the subterranean reservoir 20.

Accordingly, the EOR system 18 may include a fluid injection system 34,which has one or more tubulars 36 extending through a bore 38 in theearth 32 to the subterranean reservoir 20. For example, the EOR system18 may route one or more fluids 40, such as gas, steam, water,chemicals, or any combination thereof, into the fluid injection system34. For example, as discussed in further detail below, the EOR system 18may be coupled to the turbine-based service system 14, such that thesystem 14 routes an exhaust gas 42 (e.g., substantially or entirely freeof oxygen) to the EOR system 18 for use as the injection fluid 40. Thefluid injection system 34 routes the fluid 40 (e.g., the exhaust gas 42)through the one or more tubulars 36 into the subterranean reservoir 20,as indicated by arrows 44. The injection fluid 40 enters thesubterranean reservoir 20 through the tubular 36 at an offset distance46 away from the tubular 28 of the oil/gas well 26. Accordingly, theinjection fluid 40 displaces the oil/gas 48 disposed in the subterraneanreservoir 20, and drives the oil/gas 48 up through the one or moretubulars 28 of the hydrocarbon production system 12, as indicated byarrows 50. As discussed in further detail below, the injection fluid 40may include the exhaust gas 42 originating from the turbine-basedservice system 14, which is able to generate the exhaust gas 42 on-siteas needed by the hydrocarbon production system 12. In other words, theturbine-based system 14 may simultaneously generate one or more services(e.g., electrical power, mechanical power, steam, water (e.g.,desalinated water), and exhaust gas (e.g., substantially free ofoxygen)) for use by the hydrocarbon production system 12, therebyreducing or eliminating the reliance on external sources of suchservices.

In the illustrated embodiment, the turbine-based service system 14includes a stoichiometric exhaust gas recirculation (SEGR) gas turbinesystem 52 and an exhaust gas (EG) processing system 54. The gas turbinesystem 52 may be configured to operate in a stoichiometric combustionmode of operation (e.g., a stoichiometric control mode) and anon-stoichiometric combustion mode of operation (e.g., anon-stoichiometric control mode), such as a fuel-lean control mode or afuel-rich control mode. In the stoichiometric control mode, thecombustion generally occurs in a substantially stoichiometric ratio of afuel and oxidant, thereby resulting in substantially stoichiometriccombustion. In particular, stoichiometric combustion generally involvesconsuming substantially all of the fuel and oxidant in the combustionreaction, such that the products of combustion are substantially orentirely free of unburnt fuel and oxidant. One measure of stoichiometriccombustion is the equivalence ratio, or phi (φ), which is the ratio ofthe actual fuel/oxidant ratio relative to the stoichiometricfuel/oxidant ratio. An equivalence ratio of greater than 1.0 results ina fuel-rich combustion of the fuel and oxidant, whereas an equivalenceratio of less than 1.0 results in a fuel-lean combustion of the fuel andoxidant. In contrast, an equivalence ratio of 1.0 results in combustionthat is neither fuel-rich nor fuel-lean, thereby substantially consumingall of the fuel and oxidant in the combustion reaction. In context ofthe disclosed embodiments, the term stoichiometric or substantiallystoichiometric may refer to an equivalence ratio of approximately 0.95to approximately 1.05. However, the disclosed embodiments may alsoinclude an equivalence ratio of 1.0 plus or minus 0.01, 0.02, 0.03,0.04, 0.05, or more. Again, the stoichiometric combustion of fuel andoxidant in the turbine-based service system 14 may result in products ofcombustion or exhaust gas (e.g., 42) with substantially no unburnt fuelor oxidant remaining. For example, the exhaust gas 42 may have less than1, 2, 3, 4, or 5 percent by volume of oxidant (e.g., oxygen), unburntfuel or hydrocarbons (e.g., HCs), nitrogen oxides (e.g., NO_(X)), carbonmonoxide (CO), sulfur oxides (e.g., SO_(X)), hydrogen, and otherproducts of incomplete combustion. By further example, the exhaust gas42 may have less than approximately 10, 20, 30, 40, 50, 60, 70, 80, 90,100, 200, 300, 400, 500, 1000, 2000, 3000, 4000, or 5000 parts permillion by volume (ppmv) of oxidant (e.g., oxygen), unburnt fuel orhydrocarbons (e.g., HCs), nitrogen oxides (e.g., NO_(X)), carbonmonoxide (CO), sulfur oxides (e.g., SO_(X)), hydrogen, and otherproducts of incomplete combustion. However, the disclosed embodimentsalso may produce other ranges of residual fuel, oxidant, and otheremissions levels in the exhaust gas 42. As used herein, the termsemissions, emissions levels, and emissions targets may refer toconcentration levels of certain products of combustion (e.g., NO_(X),CO, SO_(X), O₂, N₂, H₂, HCs, etc.), which may be present in recirculatedgas streams, vented gas streams (e.g., exhausted into the atmosphere),and gas streams used in various target systems (e.g., the hydrocarbonproduction system 12).

Although the SEGR gas turbine system 52 and the EG processing system 54may include a variety of components in different embodiments, theillustrated EG processing system 54 includes a heat recovery steamgenerator (HRSG) 56 and an exhaust gas recirculation (EGR) system 58,which receive and process an exhaust gas 60 originating from the SEGRgas turbine system 52. The HRSG 56 may include one or more heatexchangers, condensers, and various heat recovery equipment, whichcollectively function to transfer heat from the exhaust gas 60 to astream of water, thereby generating steam 62. The steam 62 may be usedin one or more steam turbines, the EOR system 18, or any other portionof the hydrocarbon production system 12. For example, the HRSG 56 maygenerate low pressure, medium pressure, and/or high pressure steam 62,which may be selectively applied to low, medium, and high pressure steamturbine stages, or different applications of the EOR system 18. Inaddition to the steam 62, a treated water 64, such as a desalinatedwater, may be generated by the HRSG 56, the EGR system 58, and/oranother portion of the EG processing system 54 or the SEGR gas turbinesystem 52. The treated water 64 (e.g., desalinated water) may beparticularly useful in areas with water shortages, such as inland ordesert regions. The treated water 64 may be generated, at least in part,due to the large volume of air driving combustion of fuel within theSEGR gas turbine system 52. While the on-site generation of steam 62 andwater 64 may be beneficial in many applications (including thehydrocarbon production system 12), the on-site generation of exhaust gas42, 60 may be particularly beneficial for the EOR system 18, due to itslow oxygen content, high pressure, and heat derived from the SEGR gasturbine system 52. Accordingly, the HRSG 56, the EGR system 58, and/oranother portion of the EG processing system 54 may output or recirculatean exhaust gas 66 into the SEGR gas turbine system 52, while alsorouting the exhaust gas 42 to the EOR system 18 for use with thehydrocarbon production system 12. Likewise, the exhaust gas 42 may beextracted directly from the SEGR gas turbine system 52 (i.e., withoutpassing through the EG processing system 54) for use in the EOR system18 of the hydrocarbon production system 12.

The exhaust gas recirculation is handled by the EGR system 58 of the EGprocessing system 54. For example, the EGR system 58 includes one ormore conduits, valves, blowers, exhaust gas treatment systems (e.g.,filters, particulate removal units, gas separation units, gaspurification units, heat exchangers, heat recovery units, moistureremoval units, catalyst units, chemical injection units, or anycombination thereof), and controls to recirculate the exhaust gas alongan exhaust gas circulation path from an output (e.g., discharged exhaustgas 60) to an input (e.g., intake exhaust gas 66) of the SEGR gasturbine system 52. In the illustrated embodiment, the SEGR gas turbinesystem 52 intakes the exhaust gas 66 into a compressor section havingone or more compressors, thereby compressing the exhaust gas 66 for usein a combustor section along with an intake of an oxidant 68 and one ormore fuels 70. The oxidant 68 may include ambient air, pure oxygen,oxygen-enriched air, oxygen-reduced air, oxygen-nitrogen mixtures, orany suitable oxidant that facilitates combustion of the fuel 70. Thefuel 70 may include one or more gas fuels, liquid fuels, or anycombination thereof. For example, the fuel 70 may include natural gas,liquefied natural gas (LNG), syngas, methane, ethane, propane, butane,naphtha, kerosene, diesel fuel, ethanol, methanol, biofuel, or anycombination thereof.

The SEGR gas turbine system 52 mixes and combusts the exhaust gas 66,the oxidant 68, and the fuel 70 in the combustor section, therebygenerating hot combustion gases or exhaust gas 60 to drive one or moreturbine stages in a turbine section. In certain embodiments, eachcombustor in the combustor section includes one or more premix fuelnozzles, one or more diffusion fuel nozzles, or any combination thereof.For example, each premix fuel nozzle may be configured to mix theoxidant 68 and the fuel 70 internally within the fuel nozzle and/orpartially upstream of the fuel nozzle, thereby injecting an oxidant-fuelmixture from the fuel nozzle into the combustion zone for a premixedcombustion (e.g., a premixed flame). By further example, each diffusionfuel nozzle may be configured to isolate the flows of oxidant 68 andfuel 70 within the fuel nozzle, thereby separately injecting the oxidant68 and the fuel 70 from the fuel nozzle into the combustion zone fordiffusion combustion (e.g., a diffusion flame). In particular, thediffusion combustion provided by the diffusion fuel nozzles delaysmixing of the oxidant 68 and the fuel 70 until the point of initialcombustion, i.e., the flame region. In embodiments employing thediffusion fuel nozzles, the diffusion flame may provide increased flamestability, because the diffusion flame generally forms at the point ofstoichiometry between the separate streams of oxidant 68 and fuel 70(i.e., as the oxidant 68 and fuel 70 are mixing). In certainembodiments, one or more diluents (e.g., the exhaust gas 60, steam,nitrogen, or another inert gas) may be pre-mixed with the oxidant 68,the fuel 70, or both, in either the diffusion fuel nozzle or the premixfuel nozzle. In addition, one or more diluents (e.g., the exhaust gas60, steam, nitrogen, or another inert gas) may be injected into thecombustor at or downstream from the point of combustion within eachcombustor. The use of these diluents may help temper the flame (e.g.,premix flame or diffusion flame), thereby helping to reduce NO_(X)emissions, such as nitrogen monoxide (NO) and nitrogen dioxide (NO₂).Regardless of the type of flame, the combustion produces hot combustiongases or exhaust gas 60 to drive one or more turbine stages. As eachturbine stage is driven by the exhaust gas 60, the SEGR gas turbinesystem 52 generates a mechanical power 72 and/or an electrical power 74(e.g., via an electrical generator). The system 52 also outputs theexhaust gas 60, and may further output water 64. Again, the water 64 maybe a treated water, such as a desalinated water, which may be useful ina variety of applications on-site or off-site.

Exhaust extraction is also provided by the SEGR gas turbine system 52using one or more extraction points 76. For example, the illustratedembodiment includes an exhaust gas (EG) supply system 78 having anexhaust gas (EG) extraction system 80 and an exhaust gas (EG) treatmentsystem 82, which receive exhaust gas 42 from the extraction points 76,treat the exhaust gas 42, and then supply or distribute the exhaust gas42 to various target systems. The target systems may include the EORsystem 18 and/or other systems, such as a pipeline 86, a storage tank88, or a carbon sequestration system 90. The EG extraction system 80 mayinclude one or more conduits, valves, controls, and flow separations,which facilitate isolation of the exhaust gas 42 from the oxidant 68,the fuel 70, and other contaminants, while also controlling thetemperature, pressure, and flow rate of the extracted exhaust gas 42.The EG treatment system 82 may include one or more heat exchangers(e.g., heat recovery units such as heat recovery steam generators,condensers, coolers, or heaters), catalyst systems (e.g., oxidationcatalyst systems), particulate and/or water removal systems (e.g., gasdehydration units, inertial separators, coalescing filters, waterimpermeable filters, and other filters), chemical injection systems,solvent based treatment systems (e.g., absorbers, flash tanks, etc.),carbon capture systems, gas separation systems, gas purificationsystems, and/or a solvent based treatment system, exhaust gascompressors, any combination thereof. These subsystems of the EGtreatment system 82 enable control of the temperature, pressure, flowrate, moisture content (e.g., amount of water removal), particulatecontent (e.g., amount of particulate removal), and gas composition(e.g., percentage of CO₂, N₂, etc.).

The extracted exhaust gas 42 is treated by one or more subsystems of theEG treatment system 82, depending on the target system. For example, theEG treatment system 82 may direct all or part of the exhaust gas 42through a carbon capture system, a gas separation system, a gaspurification system, and/or a solvent based treatment system, which iscontrolled to separate and purify a carbonaceous gas (e.g., carbondioxide) 92 and/or nitrogen (N₂) 94 for use in the various targetsystems. For example, embodiments of the EG treatment system 82 mayperform gas separation and purification to produce a plurality ofdifferent streams 95 of exhaust gas 42, such as a first stream 96, asecond stream 97, and a third stream 98. The first stream 96 may have afirst composition that is rich in carbon dioxide and/or lean in nitrogen(e.g., a CO₂ rich, N₂ lean stream). The second stream 97 may have asecond composition that has intermediate concentration levels of carbondioxide and/or nitrogen (e.g., intermediate concentration CO₂, N₂stream). The third stream 98 may have a third composition that is leanin carbon dioxide and/or rich in nitrogen (e.g., a CO₂ lean, N₂ richstream). Each stream 95 (e.g., 96, 97, and 98) may include a gasdehydration unit, a filter, a gas compressor, or any combinationthereof, to facilitate delivery of the stream 95 to a target system. Incertain embodiments, the CO₂ rich, N₂ lean stream 96 may have a CO₂purity or concentration level of greater than approximately 70, 75, 80,85, 90, 95, 96, 97, 98, or 99 percent by volume, and a N₂ purity orconcentration level of less than approximately 1, 2, 3, 4, 5, 10, 15,20, 25, or percent by volume. In contrast, the CO₂ lean, N₂ rich stream98 may have a CO₂ purity or concentration level of less thanapproximately 1, 2, 3, 4, 5, 10, 15, 20, 25, or percent by volume, and aN₂ purity or concentration level of greater than approximately 70, 75,80, 85, 90, 95, 96, 97, 98, or 99 percent by volume. The intermediateconcentration CO₂, N₂ stream 97 may have a CO₂ purity or concentrationlevel and/or a N₂ purity or concentration level of between approximately30 to 70, 35 to 65, 40 to 60, or 45 to 55 percent by volume. Althoughthe foregoing ranges are merely non-limiting examples, the CO₂ rich, N₂lean stream 96 and the CO₂ lean, N₂ rich stream 98 may be particularlywell suited for use with the EOR system 18 and the other systems 84.However, any of these rich, lean, or intermediate concentration CO₂streams 95 may be used, alone or in various combinations, with the EORsystem 18 and the other systems 84. For example, the EOR system 18 andthe other systems 84 (e.g., the pipeline 86, storage tank 88, and thecarbon sequestration system 90) each may receive one or more CO₂ rich,N₂ lean streams 96, one or more CO₂ lean, N₂ rich streams 98, one ormore intermediate concentration CO₂, N₂ streams 97, and one or moreuntreated exhaust gas 42 streams (i.e., bypassing the EG treatmentsystem 82).

The EG extraction system 80 extracts the exhaust gas 42 at one or moreextraction points 76 along the compressor section, the combustorsection, and/or the turbine section, such that the exhaust gas 42 may beused in the EOR system 18 and other systems 84 at suitable temperaturesand pressures. The EG extraction system 80 and/or the EG treatmentsystem 82 also may circulate fluid flows (e.g., exhaust gas 42) to andfrom the EG processing system 54. For example, a portion of the exhaustgas 42 passing through the EG processing system 54 may be extracted bythe EG extraction system 80 for use in the EOR system 18 and the othersystems 84. In certain embodiments, the EG supply system 78 and the EGprocessing system 54 may be independent or integral with one another,and thus may use independent or common subsystems. For example, the EGtreatment system 82 may be used by both the EG supply system 78 and theEG processing system 54. Exhaust gas 42 extracted from the EG processingsystem 54 may undergo multiple stages of gas treatment, such as one ormore stages of gas treatment in the EG processing system 54 followed byone or more additional stages of gas treatment in the EG treatmentsystem 82.

At each extraction point 76, the extracted exhaust gas 42 may besubstantially free of oxidant 68 and fuel 70 (e.g., unburnt fuel orhydrocarbons) due to substantially stoichiometric combustion and/or gastreatment in the EG processing system 54. Furthermore, depending on thetarget system, the extracted exhaust gas 42 may undergo furthertreatment in the EG treatment system 82 of the EG supply system 78,thereby further reducing any residual oxidant 68, fuel 70, or otherundesirable products of combustion. For example, either before or aftertreatment in the EG treatment system 82, the extracted exhaust gas 42may have less than 1, 2, 3, 4, or 5 percent by volume of oxidant (e.g.,oxygen), unburnt fuel or hydrocarbons (e.g., HCs), nitrogen oxides(e.g., NO_(X)), carbon monoxide (CO), sulfur oxides (e.g., SO_(X)),hydrogen, and other products of incomplete combustion. By furtherexample, either before or after treatment in the EG treatment system 82,the extracted exhaust gas 42 may have less than approximately 10, 20,30, 40, 50, 60, 70, 80, 90, 100, 200, 300, 400, 500, 1000, 2000, 3000,4000, or 5000 parts per million by volume (ppmv) of oxidant (e.g.,oxygen), unburnt fuel or hydrocarbons (e.g., HCs), nitrogen oxides(e.g., NO_(X)), carbon monoxide (CO), sulfur oxides (e.g., SO_(X)),hydrogen, and other products of incomplete combustion. Thus, the exhaustgas 42 is particularly well suited for use with the EOR system 18.

The EGR operation of the turbine system 52 specifically enables theexhaust extraction at a multitude of locations 76. For example, thecompressor section of the system 52 may be used to compress the exhaustgas 66 without any oxidant 68 (i.e., only compression of the exhaust gas66), such that a substantially oxygen-free exhaust gas 42 may beextracted from the compressor section and/or the combustor section priorto entry of the oxidant 68 and the fuel 70. The extraction points 76 maybe located at interstage ports between adjacent compressor stages, atports along the compressor discharge casing, at ports along eachcombustor in the combustor section, or any combination thereof. Incertain embodiments, the exhaust gas 66 may not mix with the oxidant 68and fuel 70 until it reaches the head end portion and/or fuel nozzles ofeach combustor in the combustor section. Furthermore, one or more flowseparators (e.g., walls, dividers, baffles, or the like) may be used toisolate the oxidant 68 and the fuel 70 from the extraction points 76.With these flow separators, the extraction points 76 may be disposeddirectly along a wall of each combustor in the combustor section.

Once the exhaust gas 66, oxidant 68, and fuel 70 flow through the headend portion (e.g., through fuel nozzles) into the combustion portion(e.g., combustion chamber) of each combustor, the SEGR gas turbinesystem 52 is controlled to provide a substantially stoichiometriccombustion of the exhaust gas 66, oxidant 68, and fuel 70. For example,the system 52 may maintain an equivalence ratio of approximately 0.95 toapproximately 1.05. As a result, the products of combustion of themixture of exhaust gas 66, oxidant 68, and fuel 70 in each combustor issubstantially free of oxygen and unburnt fuel. Thus, the products ofcombustion (or exhaust gas) may be extracted from the turbine section ofthe SEGR gas turbine system 52 for use as the exhaust gas 42 routed tothe EOR system 18. Along the turbine section, the extraction points 76may be located at any turbine stage, such as interstage ports betweenadjacent turbine stages. Thus, using any of the foregoing extractionpoints 76, the turbine-based service system 14 may generate, extract,and deliver the exhaust gas 42 to the hydrocarbon production system 12(e.g., the EOR system 18) for use in the production of oil/gas 48 fromthe subterranean reservoir 20.

FIG. 2 is a diagram of an embodiment of the system 10 of FIG. 1,illustrating a control system 100 coupled to the turbine-based servicesystem 14 and the hydrocarbon production system 12. In the illustratedembodiment, the turbine-based service system 14 includes a combinedcycle system 102, which includes the SEGR gas turbine system 52 as atopping cycle, a steam turbine 104 as a bottoming cycle, and the HRSG 56to recover heat from the exhaust gas 60 to generate the steam 62 fordriving the steam turbine 104. Again, the SEGR gas turbine system 52receives, mixes, and stoichiometrically combusts the exhaust gas 66, theoxidant 68, and the fuel 70 (e.g., premix and/or diffusion flames),thereby producing the exhaust gas 60, the mechanical power 72, theelectrical power 74, and/or the water 64. For example, the SEGR gasturbine system 52 may drive one or more loads or machinery 106, such asan electrical generator, an oxidant compressor (e.g., a main aircompressor), a gear box, a pump, equipment of the hydrocarbon productionsystem 12, or any combination thereof. In some embodiments, themachinery 106 may include other drives, such as electrical motors orsteam turbines (e.g., the steam turbine 104), in tandem with the SEGRgas turbine system 52. Accordingly, an output of the machinery 106driven by the SEGR gas turbines system 52 (and any additional drives)may include the mechanical power 72 and the electrical power 74. Themechanical power 72 and/or the electrical power 74 may be used on-sitefor powering the hydrocarbon production system 12, the electrical power74 may be distributed to the power grid, or any combination thereof. Theoutput of the machinery 106 also may include a compressed fluid, such asa compressed oxidant 68 (e.g., air or oxygen), for intake into thecombustion section of the SEGR gas turbine system 52. Each of theseoutputs (e.g., the exhaust gas 60, the mechanical power 72, theelectrical power 74, and/or the water 64) may be considered a service ofthe turbine-based service system 14.

The SEGR gas turbine system 52 produces the exhaust gas 42, 60, whichmay be substantially free of oxygen, and routes this exhaust gas 42, 60to the EG processing system 54 and/or the EG supply system 78. The EGsupply system 78 may treat and delivery the exhaust gas 42 (e.g.,streams 95) to the hydrocarbon production system 12 and/or the othersystems 84. As discussed above, the EG processing system 54 may includethe HRSG 56 and the EGR system 58. The HRSG 56 may include one or moreheat exchangers, condensers, and various heat recovery equipment, whichmay be used to recover or transfer heat from the exhaust gas 60 to water108 to generate the steam 62 for driving the steam turbine 104. Similarto the SEGR gas turbine system 52, the steam turbine 104 may drive oneor more loads or machinery 106, thereby generating the mechanical power72 and the electrical power 74. In the illustrated embodiment, the SEGRgas turbine system 52 and the steam turbine 104 are arranged in tandemto drive the same machinery 106. However, in other embodiments, the SEGRgas turbine system 52 and the steam turbine 104 may separately drivedifferent machinery 106 to independently generate mechanical power 72and/or electrical power 74. As the steam turbine 104 is driven by thesteam 62 from the HRSG 56, the steam 62 gradually decreases intemperature and pressure. Accordingly, the steam turbine 104recirculates the used steam 62 and/or water 108 back into the HRSG 56for additional steam generation via heat recovery from the exhaust gas60. In addition to steam generation, the HRSG 56, the EGR system 58,and/or another portion of the EG processing system 54 may produce thewater 64, the exhaust gas 42 for use with the hydrocarbon productionsystem 12, and the exhaust gas 66 for use as an input into the SEGR gasturbine system 52. For example, the water 64 may be a treated water 64,such as a desalinated water for use in other applications. Thedesalinated water may be particularly useful in regions of low wateravailability. Regarding the exhaust gas 60, embodiments of the EGprocessing system 54 may be configured to recirculate the exhaust gas 60through the EGR system 58 with or without passing the exhaust gas 60through the HRSG 56.

In the illustrated embodiment, the SEGR gas turbine system 52 has anexhaust recirculation path 110, which extends from an exhaust outlet toan exhaust inlet of the system 52. Along the path 110, the exhaust gas60 passes through the EG processing system 54, which includes the HRSG56 and the EGR system 58 in the illustrated embodiment. The EGR system58 may include one or more conduits, valves, blowers, gas treatmentsystems (e.g., filters, particulate removal units, gas separation units,gas purification units, heat exchangers, heat recovery units such asheat recovery steam generators, moisture removal units, catalyst units,chemical injection units, or any combination thereof) in series and/orparallel arrangements along the path 110. In other words, the EGR system58 may include any flow control components, pressure control components,temperature control components, moisture control components, and gascomposition control components along the exhaust recirculation path 110between the exhaust outlet and the exhaust inlet of the system 52.Accordingly, in embodiments with the HRSG 56 along the path 110, theHRSG 56 may be considered a component of the EGR system 58. However, incertain embodiments, the HRSG 56 may be disposed along an exhaust pathindependent from the exhaust recirculation path 110. Regardless ofwhether the HRSG 56 is along a separate path or a common path with theEGR system 58, the HRSG 56 and the EGR system 58 intake the exhaust gas60 and output either the recirculated exhaust gas 66, the exhaust gas 42for use with the EG supply system 78 (e.g., for the hydrocarbonproduction system 12 and/or other systems 84), or another output ofexhaust gas. Again, the SEGR gas turbine system 52 intakes, mixes, andstoichiometrically combusts the exhaust gas 66, the oxidant 68, and thefuel 70 (e.g., premixed and/or diffusion flames) to produce asubstantially oxygen-free and fuel-free exhaust gas 60 for distributionto the EG processing system 54, the hydrocarbon production system 12, orother systems 84.

As noted above with reference to FIG. 1, the hydrocarbon productionsystem 12 may include a variety of equipment to facilitate the recoveryor production of oil/gas 48 from a subterranean reservoir 20 through anoil/gas well 26. For example, the hydrocarbon production system 12 mayinclude the EOR system 18 having the fluid injection system 34. In theillustrated embodiment, the fluid injection system 34 includes anexhaust gas injection EOR system 112 and a steam injection EOR system114. Although the fluid injection system 34 may receive fluids from avariety of sources, the illustrated embodiment may receive the exhaustgas 42 and the steam 62 from the turbine-based service system 14. Theexhaust gas 42 and/or the steam 62 produced by the turbine-based servicesystem 14 also may be routed to the hydrocarbon production system 12 foruse in other oil/gas systems 116.

The quantity, quality, and flow of the exhaust gas 42 and/or the steam62 may be controlled by the control system 100. The control system 100may be dedicated entirely to the turbine-based service system 14, or thecontrol system 100 may optionally also provide control (or at least somedata to facilitate control) for the hydrocarbon production system 12and/or other systems 84. In the illustrated embodiment, the controlsystem 100 includes a controller 118 having a processor 120, a memory122, a steam turbine control 124, a SEGR gas turbine system control 126,and a machinery control 128. The processor 120 may include a singleprocessor or two or more redundant processors, such as triple redundantprocessors for control of the turbine-based service system 14. Thememory 122 may include volatile and/or non-volatile memory. For example,the memory 122 may include one or more hard drives, flash memory,read-only memory, random access memory, or any combination thereof. Thecontrols 124, 126, and 128 may include software and/or hardwarecontrols. For example, the controls 124, 126, and 128 may includevarious instructions or code stored on the memory 122 and executable bythe processor 120. The control 124 is configured to control operation ofthe steam turbine 104, the SEGR gas turbine system control 126 isconfigured to control the system 52, and the machinery control 128 isconfigured to control the machinery 106. Thus, the controller 118 (e.g.,controls 124, 126, and 128) may be configured to coordinate varioussub-systems of the turbine-based service system 14 to provide a suitablestream of the exhaust gas 42 to the hydrocarbon production system 12.

In certain embodiments of the control system 100, each element (e.g.,system, subsystem, and component) illustrated in the drawings ordescribed herein includes (e.g., directly within, upstream, ordownstream of such element) one or more industrial control features,such as sensors and control devices, which are communicatively coupledwith one another over an industrial control network along with thecontroller 118. For example, the control devices associated with eachelement may include a dedicated device controller (e.g., including aprocessor, memory, and control instructions), one or more actuators,valves, switches, and industrial control equipment, which enable controlbased on sensor feedback 130, control signals from the controller 118,control signals from a user, or any combination thereof. Thus, any ofthe control functionality described herein may be implemented withcontrol instructions stored and/or executable by the controller 118,dedicated device controllers associated with each element, or acombination thereof.

In order to facilitate such control functionality, the control system100 includes one or more sensors distributed throughout the system 10 toobtain the sensor feedback 130 for use in execution of the variouscontrols, e.g., the controls 124, 126, and 128. For example, the sensorfeedback 130 may be obtained from sensors distributed throughout theSEGR gas turbine system 52, the machinery 106, the EG processing system54, the steam turbine 104, the hydrocarbon production system 12, or anyother components throughout the turbine-based service system 14 or thehydrocarbon production system 12. For example, the sensor feedback 130may include temperature feedback, pressure feedback, flow rate feedback,flame temperature feedback, combustion dynamics feedback, intake oxidantcomposition feedback, intake fuel composition feedback, exhaustcomposition feedback, the output level of mechanical power 72, theoutput level of electrical power 74, the output quantity of the exhaustgas 42, 60, the output quantity or quality of the water 64, or anycombination thereof. For example, the sensor feedback 130 may include acomposition of the exhaust gas 42, 60 to facilitate stoichiometriccombustion in the SEGR gas turbine system 52. For example, the sensorfeedback 130 may include feedback from one or more intake oxidantsensors along an oxidant supply path of the oxidant 68, one or moreintake fuel sensors along a fuel supply path of the fuel 70, and one ormore exhaust emissions sensors disposed along the exhaust recirculationpath 110 and/or within the SEGR gas turbine system 52. The intakeoxidant sensors, intake fuel sensors, and exhaust emissions sensors mayinclude temperature sensors, pressure sensors, flow rate sensors, andcomposition sensors. The emissions sensors may includes sensors fornitrogen oxides (e.g., NO_(X) sensors), carbon oxides (e.g., CO sensorsand CO₂ sensors), sulfur oxides (e.g., SO_(X) sensors), hydrogen (e.g.,H₂ sensors), oxygen (e.g., O₂ sensors), unburnt hydrocarbons (e.g., HCsensors), or other products of incomplete combustion, or any combinationthereof.

Using this feedback 130, the control system 100 may adjust (e.g.,increase, decrease, or maintain) the intake flow of exhaust gas 66,oxidant 68, and/or fuel 70 into the SEGR gas turbine system 52 (amongother operational parameters) to maintain the equivalence ratio within asuitable range, e.g., between approximately 0.95 to approximately 1.05,between approximately 0.95 to approximately 1.0, between approximately1.0 to approximately 1.05, or substantially at 1.0. For example, thecontrol system 100 may analyze the feedback 130 to monitor the exhaustemissions (e.g., concentration levels of nitrogen oxides, carbon oxidessuch as CO and CO₂, sulfur oxides, hydrogen, oxygen, unburnthydrocarbons, and other products of incomplete combustion) and/ordetermine the equivalence ratio, and then control one or more componentsto adjust the exhaust emissions (e.g., concentration levels in theexhaust gas 42) and/or the equivalence ratio. The controlled componentsmay include any of the components illustrated and described withreference to the drawings, including but not limited to, valves alongthe supply paths for the oxidant 68, the fuel 70, and the exhaust gas66; an oxidant compressor, a fuel pump, or any components in the EGprocessing system 54; any components of the SEGR gas turbine system 52,or any combination thereof. The controlled components may adjust (e.g.,increase, decrease, or maintain) the flow rates, temperatures,pressures, or percentages (e.g., equivalence ratio) of the oxidant 68,the fuel 70, and the exhaust gas 66 that combust within the SEGR gasturbine system 52. The controlled components also may include one ormore gas treatment systems, such as catalyst units (e.g., oxidationcatalyst units), supplies for the catalyst units (e.g., oxidation fuel,heat, electricity, etc.), gas purification and/or separation units(e.g., solvent based separators, absorbers, flash tanks, etc.), andfiltration units. The gas treatment systems may help reduce variousexhaust emissions along the exhaust recirculation path 110, a vent path(e.g., exhausted into the atmosphere), or an extraction path to the EGsupply system 78.

In certain embodiments, the control system 100 may analyze the feedback130 and control one or more components to maintain or reduce emissionslevels (e.g., concentration levels in the exhaust gas 42, 60, 95) to atarget range, such as less than approximately 10, 20, 30, 40, 50, 100,200, 300, 400, 500, 1000, 2000, 3000, 4000, 5000, or 10000 parts permillion by volume (ppmv). These target ranges may be the same ordifferent for each of the exhaust emissions, e.g., concentration levelsof nitrogen oxides, carbon monoxide, sulfur oxides, hydrogen, oxygen,unburnt hydrocarbons, and other products of incomplete combustion. Forexample, depending on the equivalence ratio, the control system 100 mayselectively control exhaust emissions (e.g., concentration levels) ofoxidant (e.g., oxygen) within a target range of less than approximately10, 20, 30, 40, 50, 60, 70, 80, 90, 100, 250, 500, 750, or 1000 ppmv;carbon monoxide (CO) within a target range of less than approximately20, 50, 100, 200, 500, 1000, 2500, or 5000 ppmv; and nitrogen oxides(NO_(X)) within a target range of less than approximately 50, 100, 200,300, 400, or 500 ppmv. In certain embodiments operating with asubstantially stoichiometric equivalence ratio, the control system 100may selectively control exhaust emissions (e.g., concentration levels)of oxidant (e.g., oxygen) within a target range of less thanapproximately 10, 20, 30, 40, 50, 60, 70, 80, 90, or 100 ppmv; andcarbon monoxide (CO) within a target range of less than approximately500, 1000, 2000, 3000, 4000, or 5000 ppmv. In certain embodimentsoperating with a fuel-lean equivalence ratio (e.g., betweenapproximately 0.95 to 1.0), the control system 100 may selectivelycontrol exhaust emissions (e.g., concentration levels) of oxidant (e.g.,oxygen) within a target range of less than approximately 500, 600, 700,800, 900, 1000, 1100, 1200, 1300, 1400, or 1500 ppmv; carbon monoxide(CO) within a target range of less than approximately 10, 20, 30, 40,50, 60, 70, 80, 90, 100, 150, or 200 ppmv; and nitrogen oxides (e.g.,NO_(X)) within a target range of less than approximately 50, 100, 150,200, 250, 300, 350, or 400 ppmv. The foregoing target ranges are merelyexamples, and are not intended to limit the scope of the disclosedembodiments.

The control system 100 also may be coupled to a local interface 132 anda remote interface 134. For example, the local interface 132 may includea computer workstation disposed on-site at the turbine-based servicesystem 14 and/or the hydrocarbon production system 12. In contrast, theremote interface 134 may include a computer workstation disposedoff-site from the turbine-based service system 14 and the hydrocarbonproduction system 12, such as through an internet connection. Theseinterfaces 132 and 134 facilitate monitoring and control of theturbine-based service system 14, such as through one or more graphicaldisplays of sensor feedback 130, operational parameters, and so forth.

Again, as noted above, the controller 118 includes a variety of controls124, 126, and 128 to facilitate control of the turbine-based servicesystem 14. The steam turbine control 124 may receive the sensor feedback130 and output control commands to facilitate operation of the steamturbine 104. For example, the steam turbine control 124 may receive thesensor feedback 130 from the HRSG 56, the machinery 106, temperature andpressure sensors along a path of the steam 62, temperature and pressuresensors along a path of the water 108, and various sensors indicative ofthe mechanical power 72 and the electrical power 74. Likewise, the SEGRgas turbine system control 126 may receive sensor feedback 130 from oneor more sensors disposed along the SEGR gas turbine system 52, themachinery 106, the EG processing system 54, or any combination thereof.For example, the sensor feedback 130 may be obtained from temperaturesensors, pressure sensors, clearance sensors, vibration sensors, flamesensors, fuel composition sensors, exhaust gas composition sensors, orany combination thereof, disposed within or external to the SEGR gasturbine system 52. Finally, the machinery control 128 may receive sensorfeedback 130 from various sensors associated with the mechanical power72 and the electrical power 74, as well as sensors disposed within themachinery 106. Each of these controls 124, 126, and 128 uses the sensorfeedback 130 to improve operation of the turbine-based service system14.

In the illustrated embodiment, the SEGR gas turbine system control 126may execute instructions to control the quantity and quality of theexhaust gas 42, 60, 95 in the EG processing system 54, the EG supplysystem 78, the hydrocarbon production system 12, and/or the othersystems 84. For example, the SEGR gas turbine system control 126 maymaintain a level of oxidant (e.g., oxygen) and/or unburnt fuel in theexhaust gas 60 below a threshold suitable for use with the exhaust gasinjection EOR system 112. In certain embodiments, the threshold levelsmay be less than 1, 2, 3, 4, or 5 percent of oxidant (e.g., oxygen)and/or unburnt fuel by volume of the exhaust gas 42, 60; or thethreshold levels of oxidant (e.g., oxygen) and/or unburnt fuel (andother exhaust emissions) may be less than approximately 10, 20, 30, 40,50, 60, 70, 80, 90, 100, 200, 300, 400, 500, 1000, 2000, 3000, 4000, or5000 parts per million by volume (ppmv) in the exhaust gas 42, 60. Byfurther example, in order to achieve these low levels of oxidant (e.g.,oxygen) and/or unburnt fuel, the SEGR gas turbine system control 126 maymaintain an equivalence ratio for combustion in the SEGR gas turbinesystem 52 between approximately 0.95 and approximately 1.05. The SEGRgas turbine system control 126 also may control the EG extraction system80 and the EG treatment system 82 to maintain the temperature, pressure,flow rate, and gas composition of the exhaust gas 42, 60, 95 withinsuitable ranges for the exhaust gas injection EOR system 112, thepipeline 86, the storage tank 88, and the carbon sequestration system90. As discussed above, the EG treatment system 82 may be controlled topurify and/or separate the exhaust gas 42 into one or more gas streams95, such as the CO₂ rich, N₂ lean stream 96, the intermediateconcentration CO₂, N₂ stream 97, and the CO₂ lean, N₂ rich stream 98. Inaddition to controls for the exhaust gas 42, 60, and 95, the controls124, 126, and 128 may execute one or more instructions to maintain themechanical power 72 within a suitable power range, or maintain theelectrical power 74 within a suitable frequency and power range.

FIG. 3 is a diagram of embodiment of the system 10, further illustratingdetails of the SEGR gas turbine system 52 for use with the hydrocarbonproduction system 12 and/or other systems 84. In the illustratedembodiment, the SEGR gas turbine system 52 includes a gas turbine engine150 coupled to the EG processing system 54. The illustrated gas turbineengine 150 includes a compressor section 152, a combustor section 154,and an expander section or turbine section 156. The compressor section152 includes one or more exhaust gas compressors or compressor stages158, such as 1 to 20 stages of rotary compressor blades disposed in aseries arrangement. Likewise, the combustor section 154 includes one ormore combustors 160, such as 1 to 20 combustors 160 distributedcircumferentially about a rotational axis 162 of the SEGR gas turbinesystem 52. Furthermore, each combustor 160 may include one or more fuelnozzles 164 configured to inject the exhaust gas 66, the oxidant 68,and/or the fuel 70. For example, a head end portion 166 of eachcombustor 160 may house 1, 2, 3, 4, 5, 6, or more fuel nozzles 164,which may inject streams or mixtures of the exhaust gas 66, the oxidant68, and/or the fuel 70 into a combustion portion 168 (e.g., combustionchamber) of the combustor 160.

The fuel nozzles 164 may include any combination of premix fuel nozzles164 (e.g., configured to premix the oxidant 68 and fuel 70 forgeneration of an oxidant/fuel premix flame) and/or diffusion fuelnozzles 164 (e.g., configured to inject separate flows of the oxidant 68and fuel 70 for generation of an oxidant/fuel diffusion flame).Embodiments of the premix fuel nozzles 164 may include swirl vanes,mixing chambers, or other features to internally mix the oxidant 68 andfuel 70 within the nozzles 164. The premix fuel nozzles 164 also mayreceive at least some partially mixed oxidant 68 and fuel 70. In certainembodiments, each diffusion fuel nozzle 164 may isolate flows of theoxidant 68 and the fuel 70 until the point of injection, while alsoisolating flows of one or more diluents (e.g., the exhaust gas 66,steam, nitrogen, or another inert gas) until the point of injection. Inother embodiments, each diffusion fuel nozzle 164 may isolate flows ofthe oxidant 68 and the fuel 70 until the point of injection, whilepartially mixing one or more diluents (e.g., the exhaust gas 66, steam,nitrogen, or another inert gas) with the oxidant 68 and/or the fuel 70prior to the point of injection. In addition, one or more diluents(e.g., the exhaust gas 66, steam, nitrogen, or another inert gas) may beinjected into the combustor (e.g., into the hot products of combustion)either at or downstream from the combustion zone, thereby helping toreduce the temperature of the hot products of combustion and reduceemissions of NO_(X) (e.g., NO and NO₂). Regardless of the type of fuelnozzle 164, the SEGR gas turbine system 52 may be controlled to providesubstantially stoichiometric combustion of the oxidant 68 and fuel 70.

In operation, as illustrated, the compressor section 152 receives andcompresses the exhaust gas 66 from the EG processing system 54, andoutputs a compressed exhaust gas 170 to each of the combustors 160 inthe combustor section 154. Upon combustion of the fuel 60, oxidant 68,and exhaust gas 170 within each combustor 160, additional exhaust gas orproducts of combustion 172 (i.e., combustion gas) is routed into theturbine section 156. Similar to the compressor section 152, the turbinesection 156 includes one or more turbines or turbine stages 174, whichmay include a series of rotary turbine blades. These turbine blades arethen driven by the products of combustion 172 generated in the combustorsection 154, thereby driving rotation of a shaft 176 coupled to themachinery 106. Again, the machinery 106 may include a variety ofequipment coupled to either end of the SEGR gas turbine system 52, suchas machinery 106, 178 coupled to the turbine section 156 and/ormachinery 106, 180 coupled to the compressor section 152. In certainembodiments, the machinery 106, 178, 180 may include one or moreelectrical generators, oxidant compressors for the oxidant 68, fuelpumps for the fuel 70, gear boxes, or additional drives (e.g. steamturbine 104, electrical motor, etc.) coupled to the SEGR gas turbinesystem 52. As illustrated, the turbine section 156 outputs the exhaustgas 60 to recirculate along the exhaust recirculation path 110 from anexhaust outlet 182 of the turbine section 156 to an exhaust inlet 184into the compressor section 152. Along the exhaust recirculation path110, the exhaust gas 60 passes through the EG processing system 54(e.g., the HRSG 56 and/or the EGR system 58) as discussed in detailabove.

Again, each combustor 160 in the combustor section 154 receives, mixes,and stoichiometrically combusts the compressed exhaust gas 170, theoxidant 68, and the fuel 70 to produce the additional exhaust gas orproducts of combustion 172 to drive the turbine section 156. In certainembodiments, the oxidant 68 is compressed by an oxidant compressionsystem 186, such as a main air compression (MAC) system. The oxidantcompression system 186 includes an oxidant compressor 188 coupled to adrive 190. For example, the drive 190 may include an electric motor, acombustion engine, or any combination thereof. In certain embodiments,the drive 190 may be a turbine engine, such as the gas turbine engine150. Accordingly, the oxidant compression system 186 may be an integralpart of the machinery 106. In other words, the compressor 188 may bedirectly or indirectly driven by the mechanical power 72 supplied by theshaft 176 of the gas turbine engine 150. In such an embodiment, thedrive 190 may be excluded, because the compressor 188 relies on thepower output from the turbine engine 150. However, in the illustratedembodiment, the oxidant compression system 186 is separate from themachinery 106. In either embodiment, the compression system 186compresses and supplies the oxidant 68 to the fuel nozzles 164 and thecombustors 160. As discussed in further detail below, the oxidant 68 andthe fuel 70 may be supplied to the gas turbine engine 150 at locationsspecifically selected to facilitate isolation and extraction of thecompressed exhaust gas 170 without any oxidant 68 or fuel 70 degradingthe quality of the exhaust gas 170.

The EG supply system 78, as illustrated in FIG. 3, is disposed betweenthe gas turbine engine 150 and the target systems (e.g., the hydrocarbonproduction system 12 and the other systems 84). In particular, the EGsupply system 78, e.g., the EG extraction system (EGES) 80), may becoupled to the gas turbine engine 150 at one or more extraction points76 along the compressor section 152, the combustor section 154, and/orthe turbine section 156. For example, the extraction points 76 may belocated between adjacent compressor stages, such as 2, 3, 4, 5, 6, 7, 8,9, or 10 interstage extraction points 76 between compressor stages. Eachof these interstage extraction points 76 provides a differenttemperature and pressure of the extracted exhaust gas 42. Similarly, theextraction points 76 may be located between adjacent turbine stages,such as 2, 3, 4, 5, 6, 7, 8, 9, or 10 interstage extraction points 76between turbine stages. Each of these interstage extraction points 76provides a different temperature and pressure of the extracted exhaustgas 42. By further example, the extraction points 76 may be located at amultitude of locations throughout the combustor section 154, which mayprovide different temperatures, pressures, flow rates, and gascompositions. Each of these extraction points 76 may include an EGextraction conduit, one or more valves, sensors, and controls, which maybe used to selectively control the flow of the extracted exhaust gas 42to the EG supply system 78.

The extracted exhaust gas 42, which is distributed by the EG supplysystem 78, has a controlled composition suitable for the target systems(e.g., the hydrocarbon production system 12 and the other systems 84).For example, at each of these extraction points 76, the exhaust gas 170may be substantially isolated from injection points (or flows) of theoxidant 68 and the fuel 70. In other words, the EG supply system 78 maybe specifically designed to extract the exhaust gas 170 from the gasturbine engine 150 without any added oxidant 68 or fuel 70. Furthermore,in view of the stoichiometric combustion in each of the combustors 160,the extracted exhaust gas 42 may be substantially free of oxygen andfuel. The EG supply system 78 may route the extracted exhaust gas 42directly or indirectly to the hydrocarbon production system 12 and/orother systems 84 for use in various processes, such as enhanced oilrecovery, carbon sequestration, storage, or transport to an offsitelocation. However, in certain embodiments, the EG supply system 78includes the EG treatment system (EGTS) 82 for further treatment of theexhaust gas 42, prior to use with the target systems. For example, theEG treatment system 82 may purify and/or separate the exhaust gas 42into one or more streams 95, such as the CO₂ rich, N₂ lean stream 96,the intermediate concentration CO₂, N₂ stream 97, and the CO₂ lean, N₂rich stream 98. These treated exhaust gas streams 95 may be usedindividually, or in any combination, with the hydrocarbon productionsystem 12 and the other systems 84 (e.g., the pipeline 86, the storagetank 88, and the carbon sequestration system 90).

Similar to the exhaust gas treatments performed in the EG supply system78, the EG processing system 54 may include a plurality of exhaust gas(EG) treatment components 192, such as indicated by element numbers 194,196, 198, 200, 202, 204, 206, 208, and 210. These EG treatmentcomponents 192 (e.g., 194 through 210) may be disposed along the exhaustrecirculation path 110 in one or more series arrangements, parallelarrangements, or any combination of series and parallel arrangements.For example, the EG treatment components 192 (e.g., 194 through 210) mayinclude any series and/or parallel arrangement, in any order, of: one ormore heat exchangers (e.g., heat recovery units such as heat recoverysteam generators, condensers, coolers, or heaters), catalyst systems(e.g., oxidation catalyst systems), particulate and/or water removalsystems (e.g., inertial separators, coalescing filters, waterimpermeable filters, and other filters), chemical injection systems,solvent based treatment systems (e.g., absorbers, flash tanks, etc.),carbon capture systems, gas separation systems, gas purificationsystems, and/or a solvent based treatment system, or any combinationthereof. In certain embodiments, the catalyst systems may include anoxidation catalyst, a carbon monoxide reduction catalyst, a nitrogenoxides reduction catalyst, an aluminum oxide, a zirconium oxide, asilicone oxide, a titanium oxide, a platinum oxide, a palladium oxide, acobalt oxide, or a mixed metal oxide, or a combination thereof. Thedisclosed embodiments are intended to include any and all permutationsof the foregoing components 192 in series and parallel arrangements. Asillustrated below, TABLE 1 depicts some non-limiting examples ofarrangements of the components 192 along the exhaust recirculation path110.

TABLE 1 194 196 198 200 202 204 206 208 210 CU HRU BB MRU PRU CU HRU HRUBB MRU PRU DIL CU HRSG HRSG BB MRU PRU OCU HRU OCU HRU OCU BB MRU PRUHRU HRU BB MRU PRU CU CU HRSG HRSG BB MRU PRU DIL OCU OCU OCU HRSG OCUHRSG OCU BB MRU PRU DIL OCU OCU OCU HRSG HRSG BB COND INER WFIL CFIL DILST ST OCU OCU BB COND INER FIL DIL HRSG HRSG ST ST OCU HRSG HRSG OCU BBMRU MRU PRU PRU ST ST HE WFIL INER FIL COND CFIL CU HRU HRU HRU BB MRUPRU PRU DIL COND COND COND HE INER FIL COND CFIL WFIL

As illustrated above in TABLE 1, a catalyst unit is represented by CU,an oxidation catalyst unit is represented by OCU, a booster blower isrepresented by BB, a heat exchanger is represented by HX, a heatrecovery unit is represented by HRU, a heat recovery steam generator isrepresented by HRSG, a condenser is represented by COND, a steam turbineis represented by ST, a particulate removal unit is represented by PRU,a moisture removal unit is represented by MRU, a filter is representedby FIL, a coalescing filter is represented by CFIL, a water impermeablefilter is represented by WFIL, an inertial separator is represented byINER, and a diluent supply system (e.g., steam, nitrogen, or other inertgas) is represented by DIL. Although TABLE 1 illustrates the components192 in sequence from the exhaust outlet 182 of the turbine section 156toward the exhaust inlet 184 of the compressor section 152, TABLE 1 isalso intended to cover the reverse sequence of the illustratedcomponents 192. In TABLE 1, any cell including two or more components isintended to cover an integrated unit with the components, a parallelarrangement of the components, or any combination thereof. Furthermore,in context of TABLE 1, the HRU, the HRSG, and the COND are examples ofthe HE; the HRSG is an example of the HRU; the COND, WFIL, and CFIL areexamples of the WRU; the INER, FIL, WFIL, and CFIL are examples of thePRU; and the WFIL and CFIL are examples of the FIL. Again, TABLE 1 isnot intended to exclude any non-illustrated permutations of thecomponents 192. In certain embodiments, the illustrated components 192(e.g., 194 through 210) may be partially or completed integrated withinthe HRSG 56, the EGR system 58, or any combination thereof. These EGtreatment components 192 may enable feedback control of temperature,pressure, flow rate, and gas composition, while also removing moistureand particulates from the exhaust gas 60. Furthermore, the treatedexhaust gas 60 may be extracted at one or more extraction points 76 foruse in the EG supply system 78 and/or recirculated to the exhaust inlet184 of the compressor section 152.

As the treated, recirculated exhaust gas 66 passes through thecompressor section 152, the SEGR gas turbine system 52 may bleed off aportion of the compressed exhaust gas along one or more lines 212 (e.g.,bleed conduits or bypass conduits). Each line 212 may route the exhaustgas into one or more heat exchangers 214 (e.g., cooling units), therebycooling the exhaust gas for recirculation back into the SEGR gas turbinesystem 52. For example, after passing through the heat exchanger 214, aportion of the cooled exhaust gas may be routed to the turbine section156 along line 212 for cooling and/or sealing of the turbine casing,turbine shrouds, bearings, and other components. In such an embodiment,the SEGR gas turbine system 52 does not route any oxidant 68 (or otherpotential contaminants) through the turbine section 156 for coolingand/or sealing purposes, and thus any leakage of the cooled exhaust gaswill not contaminate the hot products of combustion (e.g., workingexhaust gas) flowing through and driving the turbine stages of theturbine section 156. By further example, after passing through the heatexchanger 214, a portion of the cooled exhaust gas may be routed alongline 216 (e.g., return conduit) to an upstream compressor stage of thecompressor section 152, thereby improving the efficiency of compressionby the compressor section 152. In such an embodiment, the heat exchanger214 may be configured as an interstage cooling unit for the compressorsection 152. In this manner, the cooled exhaust gas helps to increasethe operational efficiency of the SEGR gas turbine system 52, whilesimultaneously helping to maintain the purity of the exhaust gas (e.g.,substantially free of oxidant and fuel).

FIG. 4 is a flow chart of an embodiment of an operational process 220 ofthe system 10 illustrated in FIGS. 1-3. In certain embodiments, theprocess 220 may be a computer implemented process, which accesses one ormore instructions stored on the memory 122 and executes the instructionson the processor 120 of the controller 118 shown in FIG. 2. For example,each step in the process 220 may include instructions executable by thecontroller 118 of the control system 100 described with reference toFIG. 2.

The process 220 may begin by initiating a startup mode of the SEGR gasturbine system 52 of FIGS. 1-3, as indicated by block 222. For example,the startup mode may involve a gradual ramp up of the SEGR gas turbinesystem 52 to maintain thermal gradients, vibration, and clearance (e.g.,between rotating and stationary parts) within acceptable thresholds. Forexample, during the startup mode 222, the process 220 may begin tosupply a compressed oxidant 68 to the combustors 160 and the fuelnozzles 164 of the combustor section 154, as indicated by block 224. Incertain embodiments, the compressed oxidant may include a compressedair, oxygen, oxygen-enriched air, oxygen-reduced air, oxygen-nitrogenmixtures, or any combination thereof. For example, the oxidant 68 may becompressed by the oxidant compression system 186 illustrated in FIG. 3.The process 220 also may begin to supply fuel to the combustors 160 andthe fuel nozzles 164 during the startup mode 222, as indicated by block226. During the startup mode 222, the process 220 also may begin tosupply exhaust gas (as available) to the combustors 160 and the fuelnozzles 164, as indicated by block 228. For example, the fuel nozzles164 may produce one or more diffusion flames, premix flames, or acombination of diffusion and premix flames. During the startup mode 222,the exhaust gas 60 being generated by the gas turbine engine 156 may beinsufficient or unstable in quantity and/or quality. Accordingly, duringthe startup mode, the process 220 may supply the exhaust gas 66 from oneor more storage units (e.g., storage tank 88), the pipeline 86, otherSEGR gas turbine systems 52, or other exhaust gas sources.

The process 220 may then combust a mixture of the compressed oxidant,fuel, and exhaust gas in the combustors 160 to produce hot combustiongas 172, as indicated by block 230. In particular, the process 220 maybe controlled by the control system 100 of FIG. 2 to facilitatestoichiometric combustion (e.g., stoichiometric diffusion combustion,premix combustion, or both) of the mixture in the combustors 160 of thecombustor section 154. However, during the startup mode 222, it may beparticularly difficult to maintain stoichiometric combustion of themixture (and thus low levels of oxidant and unburnt fuel may be presentin the hot combustion gas 172). As a result, in the startup mode 222,the hot combustion gas 172 may have greater amounts of residual oxidant68 and/or fuel 70 than during a steady state mode as discussed infurther detail below. For this reason, the process 220 may execute oneor more control instructions to reduce or eliminate the residual oxidant68 and/or fuel 70 in the hot combustion gas 172 during the startup mode.

The process 220 then drives the turbine section 156 with the hotcombustion gas 172, as indicated by block 232. For example, the hotcombustion gas 172 may drive one or more turbine stages 174 disposedwithin the turbine section 156. Downstream of the turbine section 156,the process 220 may treat the exhaust gas 60 from the final turbinestage 174, as indicated by block 234. For example, the exhaust gastreatment 234 may include filtration, catalytic reaction of any residualoxidant 68 and/or fuel 70, chemical treatment, heat recovery with theHRSG 56, and so forth. The process 220 may also recirculate at leastsome of the exhaust gas 60 back to the compressor section 152 of theSEGR gas turbine system 52, as indicated by block 236. For example, theexhaust gas recirculation 236 may involve passage through the exhaustrecirculation path 110 having the EG processing system 54 as illustratedin FIGS. 1-3.

In turn, the recirculated exhaust gas 66 may be compressed in thecompressor section 152, as indicated by block 238. For example, the SEGRgas turbine system 52 may sequentially compress the recirculated exhaustgas 66 in one or more compressor stages 158 of the compressor section152. Subsequently, the compressed exhaust gas 170 may be supplied to thecombustors 160 and fuel nozzles 164, as indicated by block 228. Steps230, 232, 234, 236, and 238 may then repeat, until the process 220eventually transitions to a steady state mode, as indicated by block240. Upon the transition 240, the process 220 may continue to performthe steps 224 through 238, but may also begin to extract the exhaust gas42 via the EG supply system 78, as indicated by block 242. For example,the exhaust gas 42 may be extracted from one or more extraction points76 along the compressor section 152, the combustor section 154, and theturbine section 156 as indicated in FIG. 3. In turn, the process 220 maysupply the extracted exhaust gas 42 from the EG supply system 78 to thehydrocarbon production system 12, as indicated by block 244. Thehydrocarbon production system 12 may then inject the exhaust gas 42 intothe earth 32 for enhanced oil recovery, as indicated by block 246. Forexample, the extracted exhaust gas 42 may be used by the exhaust gasinjection EOR system 112 of the EOR system 18 illustrated in FIGS. 1-3.

FIG. 5 is a block diagram of an embodiment of the EG processing system54 as illustrated in FIGS. 1-3. In the illustrated embodiment, the EGprocessing system 54 has the control system 100 coupled to a pluralityof gas treatment subsystems 300, valves 302, and sensors (S) 304distributed along the exhaust recirculation path 110. For example, eachsubsystem 300 and its components 192 may include one or more of thevalves 302 and the sensors 304 disposed internally within, upstream,and/or downstream of the respective subsystem 300 or component 192.Although not illustrated in FIG. 5, one or more valves 302 may belocated at or near the location of each sensor 304, thereby providinggreater flow control through the EG processing system 54. In operation,the control system 100 may obtain sensor feedback 130 from the sensors304 and provide control signals 306 to the valves 302, subsystems 300,and components 192 for control of the EG processing system 54. Thesensor feedback 130 also may include various sensor feedback from theSEGR gas turbine system 52, the EG supply system 78, and othercomponents of the turbine-based service system 14.

Each of the gas treatment subsystems 300 may include one or morecomponents to control the temperature, pressure, gas composition,moisture content, particulate content, or any combination thereof. Asillustrated in FIG. 5, the gas treatment subsystems 300 include acatalyst and heat recovery (CHR) system 308, a moisture removal system(MRS) 310, and a particulate removal system (PRS) 312. The gas treatmentsubsystems 300 also include one or more booster blowers 314 to helpincrease the flow and pressure of the exhaust gas 42 along the exhaustrecirculation path 110. Although the CHR 308, the booster blower 314,the MRS 310, and the PRS 312 are arranged in series in the illustratedembodiment, other embodiments may rearrange these components in otherseries and/or parallel configurations.

The CHR system 308 includes one or more catalyst units 316 and heatexchangers (HX) 318 disposed in series, in parallel, or integrated withone another. For example, the CHR system 308 may include a series ofcatalysts units 316, such as catalyst units 320, 322, 324, 326, and 328.The CHR system 308 also may include a series of heat exchangers 318,such as heat exchangers 330 and 332. The catalyst units 316 may be thesame or different from one another. For example, one or more of thecatalyst units 316 may include an oxidation catalyst unit (OCU) 334,which uses an oxidant fuel 336 to drive an oxidizing reaction to convertcarbon monoxide (CO) and unburnt hydrocarbons (HCs) into carbon dioxide(CO₂) and water vapor. One or more of the catalyst units 316 also maydrive a reduction reaction, which converts nitrogen oxides (NO_(X)) intocarbon dioxide (CO₂), nitrogen (N₂), and water. In the illustratedembodiment, the catalyst unit 320 is disposed upstream of the heatexchanger 330, the catalyst unit 322 is integrated within the heatexchanger 330, the catalyst unit 324 is disposed between the heatexchanger 330 and the heat exchanger 332, the catalyst unit 326 isintegrated within the heat exchanger 332, and the catalyst unit 328 isdisposed downstream from the heat exchanger 332. However, variousembodiments of the CHR system 308 may exclude or include any one or moreof the catalyst units 316, or the catalyst units 316 may be disposed inother arrangements within the CHR system 308.

The heat exchangers 318 are configured to transfer heat away from theexhaust gas 42 into one or more gases, liquids, or other fluids, such aswater. In the illustrated embodiment, each heat exchanger 318 includes aheat recovery unit (HRU) 338, which is configured to recover heat fromthe exhaust gas 42 for use in one or more other applications. Forexample, the illustrated heat recovery units 338 each include a heatrecovery steam generator (HRSG) 340, which is configured to recover heatfrom the exhaust gas 42 for the generation of steam 342. The steam 342may be used in a variety of processes within the EG processing system54, the EOR system 18, or elsewhere within the turbine-based servicesystem 14. In the illustrated embodiment, each HRSG 340 supplies thesteam 342 to one or more steam turbines (ST) 344, which may drive one ormore loads 346 to generate mechanical power 348 and/or electrical power350. For example, the loads 346 may include electrical generators, whichenable the generation of electrical power 350. Although the CHR system308 illustrates the catalyst units 316 and the heat exchangers 318 in aseries arrangement, other embodiments of the CHR system 308 may arrangetwo or more of the catalyst units 316 and the heat exchangers 318 in aparallel arrangement. After the exhaust gas 42 passes through the CHRsystem 308, the exhaust gas 42 may then flow through one or more boosterblowers 314 before passing through the moisture removal system 310 andthe particular removal system 312.

The moisture removal system (MRS) 310 may include one or more moistureremoval units (MRU) 352, such as MRUs 354 and 356. In the illustratedembodiment, the MRU 354 includes a heat exchanger 358, which may beconfigured to transfer heat away from the exhaust gas 42 into anothergas, liquid, or other fluid, thereby cooling the exhaust gas 42 formoisture removal. For example, the heat exchanger 358 may include or beconfigured as a condenser 360, which functions to cool the exhaust gas42 sufficiently to condense moisture in the exhaust gas 42 and removethe condensate as water 362. However, the MRU 354 may include a varietyof cooling units (e.g., 2, 3, 4, or more condensers, chillers, etc.) tocondense the moisture from the exhaust 42, thereby producing the water362. The MRS 310 also may include other water removal technology, suchas filtration units. For example, the MRU 356 may include one or moremoisture removal separators or filters 364, such as a water gasseparator (WGS) 366, a water impermeable filter (WFIL) 368, and acoalescing filter (CFIL) 370, which may capture and remove moisture fromthe exhaust gas 42 to produce an output of water 372. Although the MRS310 illustrates the MRU 354 upstream from the MRU 356, other embodimentsof the MRS 310 may position the MRU 356 upstream or parallel with theMRU 354. Furthermore, the MRS 310 may include additional moistureremoval filters 364, heat exchangers 358, or any other moisture removalcomponent. After the exhaust gas 42 is treated by the MRS 310 to removemoisture, the exhaust gas 42 may then pass through the particularremoval system 312.

The particulate removal system (PRS) 312 may include one or moreparticulate removal units (PRU) 374, which may be arranged in series, inparallel, or any combination thereof. For example, the PRS 312 mayinclude a PRU 376 and a PRU 378 disposed in a series arrangement. ThePRU 376 may include an inertial separator 380, a gravity separator 382,or any other type of separation unit, or any combination thereof,thereby forcing a particulate 384 to separate from a flow of the exhaustgas 42. For example, the inertial separator 380 may include acentrifugal separator, which uses centrifugal force to drive theparticulate 384 out of the flow of the exhaust gas 42. Similarly, thegravity separator 382 may use the force of gravity to drive theparticulate 384 out of the flow of the exhaust gas 42. The PRU 378 mayinclude one or more particulate removal filters 386, such as a firststage filter 388 and a second stage filter 390. These staged filters 388and 390 may include progressively finer filter media, such as membranefilters. However, the staged filters 388 and 390 may include waterimpermeable filters (WFIL), coalescing filters (CFIL), membrane filters,or any combination thereof. As the exhaust gas 42 passes through thefirst and second stage filters 388 and 390, the filters 386 capture orremove a particulate 392 from the exhaust gas 42. Although theillustrated PRS 312 has the PRU 376 upstream of the PRU 378, otherembodiments may position the PRU 378 upstream or parallel with the PRU376. After the exhaust gas 42 is treated by the PRS 312, the exhaust gas42 may then recirculate back into the SEGR gas turbine system 52, asindicated by arrow 110.

Along the exhaust recirculation path 110, the CHR system 308, the MRS310, the PRS 312, and the booster blower 314 may be controlled by thecontrol system 100 to adjust the temperature, pressure, flow rate,moisture level, particulate level, and gas composition of the exhaustgas 42 prior to entry back into the SEGR gas turbine system 52. Forexample, the control system 100 may receive the sensor feedback 130 fromvarious sensors 304 disposed along the exhaust recirculation path 110,thereby providing feedback indicative of emissions (e.g. concentrationlevels) of oxygen, carbon monoxide, hydrogen, nitrogen oxides (NO_(X)),unburnt hydrocarbons (HCs), sulfur oxides (SO_(X)), moisture, or anycombination thereof. In response to the sensor feedback 130, the controlsystem 100 may adjust (e.g., increase, decrease, or maintain) thepressure, temperature, or flow rate of the exhaust gas 66, the oxidant68, and the fuel 70 being delivered into the SEGR gas turbine system 52for combustion. For example, the control system 100 may be responsive tothe sensor feedback 130 to adjust the valves 302 along the exhaustrecirculation path 110, inlet guide vanes within the compressor section152 of the gas turbine engine 150, a vent valve 394 leading to a ventsystem 396, or any combination thereof, thereby adjusting the exhaustgas 42 flow into the combustor section 154 of the gas turbine engine150.

In the CHR system 308, the control system 100 may be responsive tosensor feedback 130 to adjust the flow of oxidant fuel 336 into each ofthe catalyst units 316, thereby increasing or decreasing the oxidizingreaction within each catalyst unit 316 to change the gas composition ofthe exhaust gas 42 that recirculates back into the SEGR gas turbinesystem 52. For example, the control system 100 may increase the flow ofoxidant fuel 336 to increase the oxidizing reaction within each UCU 334,thereby decreasing levels of carbon monoxide (CO) and unburnthydrocarbons (HCs) and increasing levels of carbon dioxide (CO₂). Thecontrol system 100 also may reduce the flow of oxidant fuel 336 intoeach of the UCUs 334, thereby decreasing the levels of carbon dioxide(CO₂) and increasing levels of carbon monoxide (CO) and unburnthydrocarbons (HCs). The control system 100 also may selectively increaseor decrease the amount of exhaust gas flow through each of the catalystunits 316, by pass one or more of the catalyst units 316, or anycombination thereof. The control system 100 also may selectively routethe exhaust gas 42 through, partially bypassing, or completelybypassing, one or more of the heat exchangers 318, such as the heatrecovery units 338. In this manner, the control system 100 may increaseor decrease the temperature of the exhaust gas 42, while also increasingor decreasing the amount of steam generation for driving the steamturbines 344.

In the MRS 310 and the PRS 312, the control system 100 may be responsiveto the sensor feedback 130 to ensure sufficient removal of moisture andparticulate. For example, in response to sensor feedback 130 indicativeof moisture content, the control system 100 may control the MRUs 352within the MRS 310 to increase or decrease the moisture removal from theexhaust gas 42. In response to sensor feedback 130 indicative ofparticulate content, the control system 100 may adjust the PRUs 374within the PRS 312, thereby increasing or decreasing the amount ofparticulate removal from the exhaust gas 42. Each of these controlactions by the control system 100 may be based on feedback 130 fromwithin the EG processing system 54, the SEGR gas turbine system 52, orelsewhere within the turbine-based service system 14. In certainembodiments, the control system 100 is configured to maintain atemperature, a pressure, and/or a flow rate of the exhaust gas 42 alongthe exhaust recirculation path 110 within a respective target range(e.g., a target temperature range, a target pressure range, and a targetflow rate range) within, upstream, or downstream of each subsystemand/or component, such as the CHR system 308, the MRS 310, the PRS 312,or any of their components (e.g., catalyst units 316, heat exchangers318, MRUs 352, PRUs 374, etc.). The control system 100 may be configuredto maintain the temperature, the pressure, and/or the flow rate withinsuch target ranges during various controlled changes in the SEGR gasturbine system 52, including changes in the flow rates of oxidant 68,fuel 70, and diluent to the fuel nozzles 164 and combustors 160.

FIG. 6 is a diagram of an embodiment of a system 420 having the EGsupply system 78 extracting, treating, and delivering the exhaust gasstreams 95 to various target system 422. As discussed above, the EGsupply system 78 includes the exhaust extraction system 80 and the EGtreatment system 82. The exhaust extraction system 80 receives theexhaust gas 42 from one or more extraction points 76 along the SEGR gasturbine system 52, the EG processing system 54, or any other locationwithin the turbine-based service system 14. The EG treatment system 82then treats the extracted exhaust gas 42 with a plurality of treatmentsubsystems 424, such as a compression system 426, a moistureremoval/dehydration system 428, a particulate removal/filtration system430, a gas separation system 432, and a gas purification system 434.

The illustrated treatment subsystems 424 may be disposed in series, inparallel, or any combination thereof. The compression system 426 mayinclude one or more rotary compressors, reciprocating compressors, orany combination thereof, in one or more compression stages. The moistureremoval/dehydration system 428 may include one or more heat exchangers,heat recovery units such as heat recovery steam generators, condensers,water gas separators such as centrifugal water gas separators, filters,desiccants or other dehydration media, or any combination thereof. Theparticulate removal/filtration system 430 may include one or moreinertial separators, gravity separators, filters, or any combinationthereof. For example, the filters may include membrane filters, waterimpermeable filters, coalescing filters, or any combination thereof. Thegas separation system 432 may include one or more solvent basedseparation systems, which may include one or more absorbers, flashtanks, or any combination thereof. For example, the gas separationsystem 432 may be configured to separate carbon dioxide (CO₂) and/ornitrogen (N₂) from the exhaust gas 42. By further example, the gasseparation system 432 may include a CO₂/N₂ separator and/or a carboncapture system. The gas purification system 432 also may include one ormore solvent based gas purifiers, and may further reduce impuritieswithin the separated gases (e.g., CO₂ and/or N₂) from the gas separationsystem 432. For example, any separated carbon dioxide (CO₂) may befurther purified by the gas purification system 434, thereby increasingpurity levels of the separated carbon dioxide (CO₂). Similarly, the gaspurification system 434 may further purify the separated nitrogen (N₂),thereby removing any impurities in the separated nitrogen (N₂). Incertain embodiments, the separated carbon dioxide and the separatednitrogen may have purity levels of at least approximately 70, 80, 90,95, 96, 97, 98, 99, or greater percentage purity by volume. In certainembodiments, the gas separation system 432 may generate the multipleexhaust gas streams 95, such as the first stream 96, the second stream97, and the third stream 98. For example, the first stream 96 mayinclude a CO₂ rich stream 436, the second stream 97 may include anintermediate concentration stream 438, and the third stream 98 mayinclude a CO₂ lean stream 440.

One or more of these exhaust gas streams 95 may then pass to one or moresecondary gas treatment systems 442 and/or energy recovery systems 444.For example, the first stream 96 may pass to a secondary gas treatmentsystem 446, the second stream 97 may pass to a secondary gas treatmentsystem 448, and the third stream 98 may pass to a secondary gastreatment system 450. Similarly, the first stream 96 may pass to anenergy recovery system 452, the second stream 97 may pass to an energyrecovery system 454, and the third stream 98 may pass to an energyrecovery system 456. Each of the secondary gas treatment system 442 mayinclude a compression system 458, a moisture removal/dehydration system460, or any other suitable treatment components. Again, the compressionsystem 458 may include one or more rotary compressors, reciprocatingcompressors, or any combination thereof, disposed in a series orparallel arrangement. The moisture removal/dehydration system 460 mayinclude water gas separators, condensers, filters, or any combinationthereof, thereby removing any moisture remaining in the streams 96, 97,or 98 after compression by the compression system 458. Again, each ofthe streams 96, 97, and 98 may pass through its own dedicated secondarygas treatment system 442, or two or more of these streams may share acommon secondary gas treatment system 442. After this secondarytreatment in the system 442, the treated exhaust gas streams 96, 97, and98 may then pass to one or more target systems 422, such as thehydrocarbon production system 12, the pipeline 86, the storage tank 88,and/or the carbon sequestration system 90. In other words, any one ormore of the individual streams 96, 97, and 98 may be independently orcollectively used by one or more of the target systems 422.

In the energy recovery systems 444, each of the streams 96, 97, and 98may enable energy recovery in one or more turbines or expanders 462,which then drive one or more loads 464 to create mechanical power 466and/or electrical power 468. For example, the load 464 may include oneor more electrical generators to produce the electrical power 468.Again, each one of the streams 96, 97, and 98 may independently orcollectively drive its own turbine or expander 462 in its own dedicatedenergy recovery system 452, 454, or 456. This recovered energy may beused to drive other equipment throughout the turbine-based servicesystem 14.

FIG. 7 is a diagram of an embodiment of the combustor section 154 of thegas turbine engine 150. As illustrated, the combustor section 154 has acasing 490 disposed about one or more combustors 160, thereby defining acompressor discharge cavity 492 between the casing 490 and the combustor160. Each combustor 160 includes the head end portion 166 and thecombustion portion 168. The combustion portion 168 may include a chamber494, a first wall or liner 496 disposed about the chamber 494, and asecond wall or flow sleeve 498 disposed at an offset around the firstwall 496. For example, the first and second walls 496 and 498 may begenerally coaxial with one another to define a hollow circumferentialspace or flow passage 500 leading from the combustion portion 168 to thehead end portion 166. The second wall or flow sleeve 498 may include aplurality of openings or perforations 502, which enables the compressedexhaust gas 170 from the compressor section 152 to enter into the flowpassage 500. The exhaust gas 170 then flows through the passage 500along the liner 496 toward the head end portion 166 as indicated byarrows 504, thereby cooling the liner 496 as the exhaust gas 170 flowstoward the head end portion 166 for delivery into the chamber 494 (e.g.through one or more fuel nozzles 164).

In certain embodiments, the liner 496 also may include one or moreopenings or perforations 506, thereby enabling injection of a portion ofthe exhaust gas 170 directly into the chamber 494 as indicated by arrows508. For example, the exhaust gas injection 508 may serve as a diluentinjection, which may be configured to control the temperature, pressure,flow rate, gas composition (e.g., emissions levels), or any combinationthereof, within the chamber 494. In particular, the exhaust gasinjection 508 may help to control the temperature within the chamber494, such that emissions of nitrogen oxides (NO_(X)) may besubstantially reduced in the hot products of combustion. One or moreadditional diluents, such as nitrogen, steam, other inert gases, oradditional exhaust gas, may be injected through one or more diluentinjectors 510, as indicated by arrows 512. Together, the exhaust gasinjection 508 and diluent injection 512 may be controlled to adjust thetemperature, concentration levels of emissions, or other characteristicsof the hot combustion gases flowing through the chamber 494.

In the head end portion 166, one or more fuel nozzles 164 may route theexhaust gas 170, the oxidant 68, the fuel 70, and one or more diluents514 (e.g., exhaust gas, steam, nitrogen, other inert gases, or anycombination thereof) into the chamber 494 for combustion. For example,each combustor 160 may include 1, 2, 3, 4, 5, 6, 7, 8, or more fuelnozzles 164, each configured as a diffusion fuel nozzle and/or a premixfuel nozzle. For example, each fuel nozzle 164 may deliver the oxidant68, the fuel 70, the diluents 514, and/or the exhaust gas 170 aspremixed or independent streams into the chamber 494, thereby generatinga flame 516. The premixed streams of oxidant 68 and fuel 70 result in apremix flame, whereas separate streams of oxidant 68 and fuel 70 resultin a diffusion flame.

The control system 100 is coupled to one or more fluid supply systems518, which control the pressure, temperature, flow rate, and/or mixturesof the oxidant 68, the fuel 70, the diluents 514, and/or the exhaust gas170. For example, the control system 100 may independently control flowsof the oxidant 68, the fuel 70, the diluents 514, and/or the exhaust gas170 in order to control the equivalence ratio, emissions levels (e.g.carbon monoxide, nitrogen oxides, sulfur oxides, unburnt hydrocarbons,hydrogen, and/or oxygen), power output, or any combination thereof. Inoperation, the control system 100 may control the fluid supply systems518 to increase the flows of oxidant 68 and fuel 70 while maintainingsubstantially stoichiometric combustion, or the control system 100 maycontrol the fluid supply systems 518 to decrease the flows of oxidant 68and fuel 70 while maintaining substantially stoichiometric combustion.The control system 100 may perform each of these increases or decreasesin flow rates of the oxidant 68 and the fuel 70 in incremental steps(e.g., 1, 2, 3, 4, 5, or more steps), continuously, or any combinationthereof. Furthermore, the control system 100 may control the fluidsupply systems 518 to increase or decrease the flows of oxidant 68 andfuel 70 in order to provide a fuel rich mixture, a fuel lean mixture, orany other mixture of the oxidant 68 and the fuel 70, into the chamber494, thereby creating hot products of combustion or exhaust gas 520 witha low oxygen concentration, a high oxygen concentration, or any othersuitable concentration of oxygen, unburnt hydrocarbons, carbon monoxide,nitrogen oxides, sulfur oxides, and so forth. While controlling theflows of oxidant 68 and fuel 70, the control system 100 also may controlthe fluid supply system 518 to increase or decrease flow of the diluents514 (e.g., steam, exhaust gas, nitrogen, or any other inert gas),thereby helping to control the temperature, pressure, flow rate, and/orgas composition (e.g., emissions levels) of the hot products ofcombustion 520 passing through the chamber 494 toward the turbinesection 156.

The control system 100 also may control the EG supply system 78,including the EG extraction system 80 and the EG treatment system 82.For example, the control system 100 may selectively open or close one ormore valves 522 disposed along extraction lines 524 between thecombustor section 154 and the EG extraction system 80. The controlsystem 100 may selectively open or close these valves 522 to increase ordecrease the flow of exhaust gas 42 to the EG extraction system 80,while also selectively extracting the exhaust gas from differentlocations resulting in different temperatures and/or pressures of theexhaust gas being delivered to the EG extraction system 80. The controlsystem 100 also may control one or more valves 526 disposed along lines528 leading to a vent system 530. For example, the control system 100may selectively open the valve 526 to vent a portion of the exhaust gasthrough the vent system 530 into the atmosphere, thereby reducing thepressure in the EG supply system 78.

As discussed above, each combustor 160 in the combustor section 154 mayinclude one or more fuel nozzles 164, which may be configured as premixfuel nozzles and/or diffusion fuel nozzles. For example, FIGS. 8, 9, and10 illustrate embodiments of the fuel nozzle 164 configured as a premixfuel nozzle 550 operable to generate a premix flame 516, 552, whereasFIGS. 11-16 illustrate embodiments of the fuel nozzle 164 configured asa diffusion fuel nozzle 554 operable to generate a diffusion flame 516,556. These fuel nozzles 550 and 554 may be used alone or in anycombination with one another in each of the combustors 160, as discussedin further detail below with reference to FIG. 17. For example, eachcombustor 160 may include only premix fuel nozzles 550, only diffusionfuel nozzles 554, or any combination of both premix fuel nozzles 550 anddiffusion fuel nozzles 554.

The premix fuel nozzles 550 may have a variety of configurations tocompletely or partially premix the oxidant 68 and the fuel 70, whilealso optionally premixing one or more diluents 514 such as the exhaustgas 170, steam, nitrogen, or any other suitable inert gas. FIG. 8 is adiagram of an embodiment of the premix fuel nozzle 550 having a mixingportion 558 coupled to an injection portion 560. The mixing portion 558includes at least one mixing chamber 562 surrounded by at least oneenclosure 564, while the injection portion 560 includes at least oneinjection passage 566 surrounded by at least one conduit 568. Forexample, the enclosure 564 of the mixing portion 558 may include one ormore conduits, injection holes, swirl vanes, flow interruptions, orother structures to facilitate mixing between the oxidant 68 and thefuel 70. The mixing portion 558 also may receive one or more flows ofthe diluents 514, such as exhaust gas 170, steam, nitrogen, or anotherinert gas, thereby mixing the diluent 514 along with the oxidant 68 andthe fuel 70. Once the oxidant 68 and the fuel 70 are sufficiently mixedwithin the mixing chamber 562, the premix fuel nozzle 550 routes thefuel oxidant mixture through the injection passage 566 to at least oneinjection outlet 570. The exiting mixture of oxidant 68 and fuel 70 (andoptionally one or more diluents 514) may then ignite to create thepremix flame 552. In certain embodiments, the control system 100 mayselectively control the fluid supply system 518 to increase or decreaseflows of the oxidant 68 and the fuel 70 (and optionally one or morediluents 514), thereby adjusting the equivalence ratio, emissions levelsgenerated by the premix flame 552, power output of the gas turbineengine 150, or any combination thereof. In certain embodiments, theillustrated premix fuel nozzle 550 may not premix any diluent with theoxidant 68 and fuel 70, but rather one or more diluents (e.g., exhaustgas, steam, nitrogen, or another inert gas) may be provided after thepoint of combustion and/or downstream from the premix flame 552. In thismanner, the flows of oxidant 68 and fuel 70 may be independentlycontrolled to provide a more precise control of the fuel/oxidant ratio,thereby helping to achieve stoichiometric combustion for improved flamestability while also using the downstream diluents for control of thetemperature and emissions (e.g., NO_(X) emissions).

FIG. 9 is a diagram of an embodiment of the premix fuel nozzle 550having a multi-stage configuration of the mixing portion 558. Asillustrated, the mixing portion 558 includes first and second mixingchambers 580 and 582, which are defined by first and second enclosureportions 584 and 586 of the enclosure 564. The first and second mixingchamber 580 and 582 are illustrated in a series configuration, althoughother embodiments of the mixing portion 558 may arrange the first andsecond mixing chambers 580 and 582 in a parallel configuration. Themixing portion 558 also may include additional mixing chambers incombination with the first and second mixing chambers 580 and 582. Forexample, the mixing portion 558 may include 1, 2, 3, 4, 5, 6, 7, 8, 9,10, or more mixing chambers in a series configuration, a parallelconfiguration, or a combination thereof. Each mixing chamber 580 and 582may include one or more mixing devices, such as swirl vanes, flowinterruptions, tortuous pathways, passages with increasing anddecreasing diameters, or any combination thereof. In operation, themixing portion 558 receives one or more flows of the oxidant 68, thefuel 70, and one or more diluents 514 from the fluid supply system 518.Again, the diluents 514 may include the exhaust gas 170, steam,nitrogen, or one or more other inert gases. Each mixing chamber 580 and582 may receive and mix two or more different fluids from the fluidsupply system 518. For example, the first mixing chamber 580 may receiveand mix one or more streams of the oxidant 68 and the fuel 70, while thesecond mixing chamber 582 may receive and mix one or more streams of theoxidant 68 and the diluents 514 or the fuel 70 and the diluents 514. Inother words, the first and second mixing chambers 580 and 582 mayreceive and mix two or more of the same fluid streams, or two or moredifferent fluid streams from the fluid supply system 518. In thismanner, the first and second mixing chambers 580 and 582 maysequentially mix the various fluids from the fluid supply system 518,and then direct the mixture into the injection passage 566 for deliveryinto the chamber 494 of the combustor 160. As the mixture of oxidant 68,fuel 70, and one or more diluents 514 flows through the injection outlet570 of the injection passage 566, the mixture ignites and forms thepremix flame 552. Again, the control system 100 may selectively controlthe fluid supply system 518 to increase, decrease, or maintain flows ofthe oxidant 68, the fuel 70, and one or more diluents 514, therebyadjusting the equivalence ratio, emissions levels, power output of thegas turbine engine 150, or any combination thereof.

FIG. 10 is a diagram of an embodiment of the premix fuel nozzle 550having a staged mixing portion 558 with a parallel mixing section 590 inseries with a swirling section 592. The parallel mixing section 590includes the first and second mixing chambers 580 and 582 as discussedabove with reference to FIG. 9, wherein the first and second mixingchambers 580 and 582 are disposed parallel with one another upstreamfrom the swirling section 592. The swirling section 592 includes aninner conduit or hub 594, an outer conduit 596 disposed about the innerconduit 594, and a plurality of swirl vanes 598 extending radiallybetween the inner conduit 594 and the outer conduit 596. Each of theswirl vanes 598 may be angled or curved to force the fluid flow to swirlin a circumferential direction 600 about a longitudinal axis 602 of thepremix fuel nozzle 550. The inner conduit 594 defines an inner passage604, the outer conduit 596 defines an outer passage 606, and each swirlvane 598 defines a radial passage 608. One or more of the swirl vanes598 also include a plurality of injection ports 610, which may bedisposed directly on or upstream from a trailing edge of each swirl vane598.

In the illustrated embodiment, the fluid supply system 518 routes one ormore flows of the oxidant 68 and the diluent 514 into the first mixingchamber 580, while also delivering one or more flows of the fuel 70 andthe diluent 514 into the second mixing chamber 582. The first mixingchamber 580 substantially mixes the flows of oxidant 68 and diluent 514,and then routes the mixture into the outer passage 606 between the innerand outer conduits 594 and 596 as indicated by arrows 612. The mixture614 of oxidant 68 and diluent 514 then flows toward the plurality ofswirl vanes 598 in the swirling section 592, where the swirl vanes 598force the mixture 614 to swirl about the axis 602 as indicated by arrow600.

Simultaneously, the second mixing chamber 582 routes a premixed flow ofthe fuel 70 and the diluent 514 into the inner passage 604 defined bythe inner conduit 594 as indicated by arrow 616. The mixture 618 of fuel70 and diluent 514 then flows lengthwise along the inner passage 604,and then turns radially into the plurality of swirl vanes 598 asindicated by arrows 620. Upon reaching the plurality of injection ports610, the mixture 618 of fuel 70 and diluent 514 then passes through theinjection ports 610 into the outer passage 606 as indicated by arrows622. The two mixtures (i.e., the premixed oxidant and diluent flow 614and the premixed fuel and diluent flow 622) then further mix within theinjection passage 566 as indicated by arrows 624. The mixture 624 ofoxidant 68, fuel 70, and diluent 514 then exits the premix fuel nozzle550 through the injection outlet 570, and subsequently ignites to formthe premix flame 552. Again, the control system 100 may selectivelycontrol the fluid supply system 518 to independently control flows ofthe oxidant 68, the fuel 70, and the diluent 514, thereby increasing,decreasing, or maintaining the equivalence ratio, emissions levels,power output, or any combination thereof, of the gas turbine engine 150.

FIG. 11 is a diagram of an embodiment of the diffusion fuel nozzle 554having a plurality of independent passages 640 for delivery of theoxidant 68 and the fuel 70 into the chamber 494 of the combustor 160.The independent passages 640 may include a plurality of concentricannular passages, a central passage surrounded by a plurality ofperipheral passages, or any combination thereof. In the illustratedembodiment, the independent passages 640 include one or more fuelpassages 642 and one or more oxidant passages 644. For example, theillustrated fuel passage 642 is a central fuel passage surrounded by aninner conduit 646, while the one or more oxidant passages 644 are outeroxidant passages disposed between the inner conduit 646 and an outerconduit or structure 648. By further example, the oxidant passage 644may include a single annular oxidant passage or a plurality of discreteoxidant passages disposed circumferentially about the fuel passage 642between the inner and outer conduits 646 and 648. In these embodiments,the oxidant and fuel passages 642 and 644 remain isolated from oneanother along a full length of the diffusion fuel nozzle 554. The innerand outer conduits 646 and 648 may function as isolation walls, whichmaintain the separation between the oxidant 68 and fuel 70. The fuelpassage 642 terminates at a fuel outlet 650 and the one or more oxidantpassages 644 terminate at one or more oxidant outlet 652. These fuel andoxidant outlets 650 and 652 may be disposed along a common plane ordownstream end 654 of the diffusion fuel nozzle 554, thereby delayingmixing of the oxidant 68 and the fuel 70 until after injection from thefuel nozzle 554 into the chamber 494 of the combustor 160.

As the oxidant 68 and the fuel 70 mix or diffuse with one another in thechamber 494, the diffusion flame 556 forms as indicated by an outline orborder 656. The outline 656 may represent a diffusion wall or flamewall, where the oxidant 68 and the fuel 70 mix and combust in asubstantially stoichiometric manner (e.g., substantially stoichiometriccombustion). In other words, the outline or border 656 may represent astable flame wall of the diffusion flame 556, wherein the equivalenceratio is approximately 1.0 or between approximately 0.95 to 1.05.Similar to the premix fuel nozzles 550 discussed above with reference toFIGS. 8-10, the diffusion fuel nozzle 554 may be controlled by thecontrol system 100 to vary the equivalence ratio, exhaust emissions,power output of the gas turbine engine 150, or any combination thereof.For example, the illustrated control system 100 selectively controls thefluid supply system 518 to increase, decrease, or maintain flows of theoxidant 68 and the fuel 70 in response to the sensor feedback 130.

FIG. 12 is a diagram of an embodiment of the diffusion fuel nozzle 554having a plurality of independent passages 670 with an injection portion672 and a mixing portion 674. The mixing portion 674 may include one ormore inner mixing chambers 676 and one or more outer mixing chambers678. For example, the inner mixing chambers 676 may be fuel/diluentmixing chambers, which are configured to mix one or more streams of thefuel 70 and the diluent 514. The outer mixing chambers 676 may includeone or more oxidant/diluent mixing chambers, which are configured to mixone or more streams of the oxidant 68 and the diluent 514. Each of thesemixing chambers may include a surrounding structure, such as an outerenclosure or conduit. For example, the mixing chambers 676 may besurrounded by an inner conduit or enclosure 680, while the mixingchambers 678 may be surrounded by an outer conduit or enclosure 682. Incertain embodiments, the mixing chamber 678 may be enclosed between theinner and outer conduits 680 and 682.

Similarly, the injection portion 672 includes one or more fuel-diluentpassages 684 and one or more oxidant-diluent passages 686. Eachfuel-diluent passage 684 is fluidly coupled to one or more of the mixingchambers 678, while each of the oxidant-diluent passages 686 is fluidlycoupled to one or more of the mixing chambers 678. The fuel-diluentpassage 684 may be surrounded by an inner conduit 688, while the one ormore oxidant-diluent passages 686 may be surrounded by an outer conduit690. For example, the illustrated fuel-diluent passage 684 may be acentral fuel-diluent passage 684, which is surrounded by one or moreouter oxidant-diluent passages 686. For example, the inner and outerconduits 688 and 690 may be concentric annular conduits, which definethe passages 684 and 686 in a coaxial or concentric annular arrangement.However, the fuel-diluent passage 684 may represent a single centralpassage or a plurality of separate passages disposed within the innerconduit 688. Likewise, the oxidant-diluent passages 686 may represent asingle annular passage or a plurality of discrete passages spaced apartfrom one another circumferentially around the fuel-diluent passage 684,while remaining isolated from one another by the inner and outerconduits 688 and 690. In certain embodiments, the inner conduits 680 and688 form a single continuous inner conduit, and the outer conduits 682and 690 form a single continuous outer conduit.

In operation, the control system 100 selectively controls the fluidsupply system 518 to increase, decrease, or maintain flows of the fuel70 and the diluent 514 into the mixing chamber 676, which mixes the fuel70 and diluent 514 before passing the mixture into the fuel-diluentpassage 684. Similarly, the control system 100 selectively controls thefluid supply system 518 to increase, decrease, or maintain flows of theoxidant 68 and the diluent 514 into the one or more mixing chambers 678,which mix the oxidant 68 and the diluent 514 before delivering themixture into the one or more oxidant-diluent passages 686. The diffusionfuel nozzle 554 then separately flows the fuel-diluent mixture 698 alongthe passage 684 to an outlet 692, while simultaneously flowing theoxidant-diluent mixture 700 along the passages 686 to one or moreoutlets 694. Similar to the embodiment of FIG. 11, the outlets 692 and694 may be arranged along a common plane or downstream end 696 of thediffusion fuel nozzle 554, thereby maintaining isolation between theoxidant-diluent mixture 700 in the passage 686 and the fuel-diluentmixture 698 in the passage 684. This isolation delays mixing between theoxidant 68 and the fuel 70 until downstream of the common plane 696.

As the fuel-diluent mixture 698 and the oxidant-diluent mixture 700 flowfrom the diffusion fuel nozzle 554 into the chamber 494 of the combustor160, the mixtures 698 and 700 generally diffuse with one another andcombust along an outline or border 702, which may define a diffusionwall or flame wall of the diffusion flame 556. Again, the control system100 may selectively control the fluid supply system 518 to independentlycontrol flows of the oxidant 68, the fuel 70, and the diluent 514 toeach of the mixing chambers 676 and 678, thereby controlling mixingwithin each of the mixing chambers 676 and 678 while also controllingthe diffusion and combustion within the chamber 494 of the combustor160. For example, the control system 100 may selectively control thefluid supply system 518 to adjust the ratio of the oxidant 68 relativeto the fuel 70, the ratio of the diluent 514 relative to the combinedflow of the oxidant 68 and the fuel 70, the ratio of the oxidant 68relative to the diluent 514 in each of the one or more mixing chambers678 and corresponding passages 686, and the ratio of the fuel 70relative to the diluent 514 in each of the one or more mixing chambers676 and corresponding passages 684. Thus, the control system 100 mayadjust each of these ratios, flow rates, temperatures, and fluidcompositions (e.g., compositions of the oxidant 68, the fuel 70, and thediluent 514) to adjust the equivalence ratio, the exhaust emissions, andthe power output of the gas turbine engine 150.

FIG. 13 is a diagram of an embodiment of the diffusion fuel nozzle 554,illustrating a plurality of independent passages 720. The illustratedpassages 640 include a fluid A passage 722, one or more fluid B passages724, and one or more fluid C passages 726. The fluid A passage 722 maybe separated or isolated from the one or more fluid B passages 724 by aconduit or structure 728, the one or more fluid B passages 724 may beseparated from the one or more fluid C passages 726 by a conduit orstructure 730, and the one or more fluid C passages 726 may besurrounded or supported by an outer conduit or structure 732.

For example, as illustrated in FIG. 14, the fluid passages 722, 724, and726 may be disposed in a concentric arrangement, wherein the conduit 728surrounds the fluid A passage 722 as a central fluid passage, the fluidB passage 724 is disposed between the conduits 728 and 730, and fluid Cpassage 726 is disposed between the conduits 730 and 732. Again, theconduits 728, 730, and 732 may be disposed in a concentric arrangement,such that the fluid B passage 724 and fluid C passage 726 each representa continuous annular passage.

However, the diffusion fuel nozzle 554 may arrange the passages 722,724, and 726 in other arrangements, such as discrete passages asillustrated in FIG. 15. In the embodiment of FIG. 15, the fluid Apassage 722 represents a central fluid passage, while the fluid Bpassages 724 and the fluid C passages 726 represent a plurality ofdiscrete passages that are spaced apart from one another within the fuelnozzle 554. For example, the fluid B passages 724 may include 2, 3, 4,5, 6, 7, 8, or more discrete fluid passages that are spaced apart fromone another circumferentially about the central fluid A passage 722.Likewise, the fluid C passages 726 may include a plurality of discretepassages that are spaced apart from one another circumferentially aboutthe fluid B passages 724. For example, the fluid B passages 724 may bearranged in a first ring or circular pattern of the passages 724, whilethe fluid C passages 726 may be arranged in a second ring or circularpattern of the passages 726.

In either of these configurations, the diffusion fuel nozzle 554 of FIG.13 is configured to separately flow a fluid A 734 through the fluid Apassage 722, a fluid B 736 through the one or more fluid B passages 724,and a fluid C 738 through the one or more fluid C passages 726. Each ofthese fluids 734, 736, and 738 may include one or more fluids, such asthe oxidant 68, the fuel 70, and the diluents 514. However, the fluids734, 736, and 738 may not mix any of the oxidant 68 and the fuel 70within the diffusion fuel nozzle 554, thereby delaying mixing betweenthe oxidant 68 and the fuel 70 until the fluids eject from openings 740,742, and 744 into the chamber 494 of the combustor 160. Again, theseopenings 740, 742, and 744 may be disposed along a common plane ordownstream end 746 of the diffusion fuel nozzle 554. The various fluidsthen mix and combust to form the diffusion flame 556, as discussedabove. The following TABLE 2 illustrates some possible non-limitingexamples of fluids A, B, and C, which may be used with the diffusionfuel nozzle 554 of FIGS. 13-15.

TABLE 2 FLUID A (722) FLUID B (724) FLUID C (726) FUEL OXIDANT DILUENTFUEL DILUENT OXIDANT FUEL OXIDANT + DILUENT OXIDANT FUEL OXIDANTOXIDANT + DILUENT FUEL + DILUENT FUEL OXIDANT FUEL FUEL + DILUENTOXIDANT FUEL + DILUENT OXIDANT + DILUENT OXIDANT FUEL + DILUENT OXIDANTOXIDANT + DILUENT FUEL OXIDANT + DILUENT OXIDANT + DILUENT

As indicated above, the diffusion fuel nozzle 554 may flow a variety ofcombinations of fluids (e.g., oxidant 68, fuel 70, and diluent 514)through the passages 722, 724, and 726 for generation of a diffusionflame 556. Again, the oxidant 68 may include oxygen, ambient air, oxygenenriched air, oxygen reduced air, mixtures of nitrogen and oxygen, orany combination thereof. The fuel 70 may include liquid fuel and/or gasfuel, such as natural gas, syngas, or any other fuel described herein.The diluent 514 may include the exhaust gas 170, steam, nitrogen, oranother inert gas, or any combination thereof. Although TABLE 2 depictssome possible examples of the fluids, any combination of fluids may beused with the diffusion fuel nozzle 554 of FIGS. 13-15. In addition,although the depicted embodiment does not mix any fuel 70 with oxidant68 within the diffusion fuel nozzle 554, other embodiments may mix asmall amount (e.g., less than 1, 2, 3, 4, 5, 6, 7, 8, 9, or 10 percentby volume) of oxidant 68 with fuel 70 or a small amount (e.g., less than1, 2, 3, 4, 5, 6, 7, 8, 9, or 10 percent by volume) of fuel 70 withoxidant 68.

FIG. 16 is a diagram of an embodiment of the combustor section 154having one of the diffusion fuel nozzles 554 disposed within thecombustor 160. Similar to the diffusion fuel nozzle 554 illustrated inFIGS. 13-15, the diffusion fuel nozzle 554 of FIG. 16 includes the fluidA passage 724 surrounded by the conduit 728, the fluid B passage 724surrounded by the conduit 730, the fluid C passage 726 surrounded by theconduit 732, and a fluid D passage 760 surrounded by an outer conduit orstructure 762. The fluid D passage 760 is configured to receive a fluidD 764 from the fluid supply system 518, and route the fluid D 764 intothe chamber 494 through one or more outlets 766. The passages 722, 724,726, and 760 may have the respective outlets 740, 742, 744, and 766disposed along the common plane or downstream end 746 of the diffusionfuel nozzle 554, thereby isolating the flows of the fluids 734, 736,738, and 764 until the fluids reach the chamber 494. In this manner, thediffusion fuel nozzle 554 facilitates the formation of the diffusionflame 556. Each of the fluids 734, 736, 738, and 764 may include theoxidant 68, the fuel 70, and one or more diluents 514, such as theexhaust gas 170, steam, nitrogen, and/or one or more other inert gases.However, the fluid passages 722, 724, 726, and 760 may not mix any ofthe oxidant 68 and the fuel 70 within the diffusion fuel nozzle 554,thereby facilitating isolation of the oxidant 68 and fuel 70 until thefluids reach the chamber 494. The oxidant 68 and the fuel 70 may flowthrough each of the independent fluid passages 722, 724, 726, and 760,either separately or partially premixed with one or more of the diluents514. Similar to the previous embodiments, the control system 100 mayselectively control the fluid supply system 518 to increase, decrease,or maintain the flows of each fluid 734, 736, 738, and 764, therebyadjusting the fluid flow ratios among the fluids, the equivalence ratio,the emissions level, the power output of the gas turbine engine 150, orany combination thereof.

The illustrated combustor 160 of FIG. 16 also includes a diluentinjection system 770 disposed along the combustion portion 168 of thecombustor 160, such that one or more diluents (e.g., exhaust gas 170,steam, nitrogen, or other inert gases) may be injected into the chamber494 to control the temperature, pressure, flow rate, gas composition(e.g., emissions levels), or any combination thereof, of the hotproducts of combustion 772 formed by the diffusion flame 556. Forexample, the diluent injection system 770 may include the openings ofperforations 506 disposed in the first wall or liner 496, and aplurality of the diluent injectors 510 extending through the first andsecond walls 496 and 498 to the chamber 494 of the combustor 160. Inoperation, the openings or perforations 506 may be configured to injecta fluid E 774, such as the exhaust gas 170, as indicated by arrows 508.The diluent injectors 510 may be configured to inject a fluid F 776and/or a fluid G 778 into the chamber 494, as indicated by arrows 512.For example, the fluid F 776 and the fluid G 778 may include additionalexhaust gas 170, steam, nitrogen, one or more other inert gases, or anycombination thereof. These injected diluents 508 and 512 may beconfigured to control the temperature, pressure, flow rate, gascomposition (e.g., emissions levels), or any combination thereof, of thehot products of combustion 772 resulting from the diffusion flame 556.In certain embodiments, the control system 100 may selectively controlthe fluid supply systems 518 to increase, decrease, or maintain flows ofthe various fluids 734, 736, 738, 764, 774, 776, and 778, therebycontrolling the ratio of the oxidant 68 to fuel 70, the ratio of one ormore diluents 514 relative to the oxidant 68 and the fuel 70, or anycombination thereof. In turn, these control adjustments of the fluidsmay alter the equivalence ratio, emissions levels, and power output ofthe gas turbine engine 150. The following TABLE 3 illustrates somepossible non-limiting examples of fluids A, B, C, D, E, F, and G, whichmay be used with the diffusion fuel nozzle 554 and combustor 160 of FIG.16.

TABLE 3 FLUID A FLUID B FLUID C FLUID D FLUID E FLUID F FLUID G (722)(724) (726) (764) (774) (776) (778) FUEL FUEL OXIDANT OXIDANT DILUENTDILUENT DILUENT FUEL OXIDANT FUEL OXIDANT DILUENT DILUENT DILUENTOXIDANT FUEL OXIDANT FUEL DILUENT DILUENT DILUENT FUEL + FUEL +OXIDANT + OXIDANT + DILUENT DILUENT DILUENT DILUENT DILUENT DILUENTDILUENT FUEL + OXIDANT + FUEL + OXIDANT + DILUENT DILUENT DILUENTDILUENT DILUENT DILUENT DILUENT OXIDANT + FUEL + OXIDANT + FUEL +DILUENT DILUENT DILUENT DILUENT DILUENT DILUENT DILUENT DILUENT FUELFUEL + OXIDANT + DILUENT OXIDANT DILUENT DILUENT DILUENT DILUENT OXIDANTOXIDANT + FUEL + DILUENT FUEL DILUENT DILUENT DILUENT FUEL OXIDANT FUELOXIDANT DILUENT FUEL DILUENT

As indicated above, the diffusion fuel nozzle 554 and combustor 160 mayflow a variety of combinations of fluids (e.g., oxidant 68, fuel 70, anddiluent 514) through the passages 722, 724, 726, and 760, openings 506,and diluent injectors 510 for generation of a diffusion flame 556.Again, the oxidant 68 may include oxygen, ambient air, oxygen enrichedair, oxygen reduced air, mixtures of nitrogen and oxygen, or anycombination thereof. The fuel 70 may include liquid fuel and/or gasfuel, such as natural gas, syngas, or any other fuel described herein.The diluent 514 may include the exhaust gas 170, steam, nitrogen, oranother inert gas, or any combination thereof. Although TABLE 3 depictssome possible examples of the fluids, any combination of fluids may beused with the diffusion fuel nozzle 554 and combustor 160 of FIG. 16. Inaddition, although the depicted embodiment does not mix any fuel 70 withoxidant 68 within the diffusion fuel nozzle 554, other embodiments maymix a small amount (e.g., less than 1, 2, 3, 4, 5, 6, 7, 8, 9, or 10percent by volume) of oxidant 68 with fuel 70 or a small amount (e.g.,less than 1, 2, 3, 4, 5, 6, 7, 8, 9, or 10 percent by volume) of fuel 70with oxidant 68.

FIG. 17 is a schematic cross-section of the combustor 160 taken alongline 17-17 of FIG. 7, further illustrating a multi-nozzle arrangement ofthe fuel nozzles 164 and a multi-injector arrangement of the diluentinjectors 510. The illustrated fuel nozzles 164 include a fuel nozzle A790, a fuel nozzle B 792, a fuel nozzle C 794, a fuel nozzle D 796, afuel nozzle E 798, a fuel nozzle F 800, and a fuel nozzle G 802. In theillustrated embodiment, the nozzle 790 is a central fuel nozzle, whichis surrounded by the remaining fuel nozzles 792, 794, 796, 798, 800 and802 as outer or peripheral fuel nozzles. Although the illustratedembodiment includes a single central fuel nozzle 164 and six outer fuelnozzles 164, other embodiments may include any number of central andouter fuel nozzles. The illustrated fuel nozzles 164 may include one ormore of the premix fuel nozzles 550 and/or the diffusion fuel nozzles554 shown and described with reference to FIGS. 8-16. For example, allof the fuel nozzles 164 may be configured as premix fuel nozzles 550,all of the fuel nozzles 164 may be configured as diffusion fuel nozzles554, or the fuel nozzles 164 may include one or more of both the premixfuel nozzles 550 and the diffusion fuel nozzles 554. The fluid flows tothe fuel nozzles 164 may be independently controlled for each fuelnozzle 164, or the fluid flows may be controlled in groups of fuelnozzles 164. For example, the central fuel nozzle 790 may be controlledindependently from one or more groups of the outer fuel nozzles 792,794, 796, 798, 800, and 802. By further example, one or more premix fuelnozzles 550 may be controlled independently from one or more diffusionfuel nozzles 554. These different control schemes may facilitatedifferent operations modes, which may be useful in providingstoichiometric combustion and reducing emissions in the exhaust gas 42.

As further illustrated in FIG. 17, the fuel nozzles 164 and diluentinjectors 510 may be coupled to the fluid supply system 518 through aplurality of fluid supply circuits 810, such as one or more diluentsupply circuits 812 and one or more fuel nozzle supply circuits 814. Forexample, the diluent supply circuits 812 may include 1, 2, 3, 4, 5, 6,7, 8, or more independent diluent supply circuits 812, thereby enablinga variety of diluent injection modes for the diluent injectors 510.Similarly, the fuel nozzle supply circuits 814 may include 1, 2, 3, 4,5, 6, 7, 8, or more independent fuel nozzle supply circuits 814, therebyenabling a variety of fluid supply modes for the fuel nozzles 164. Forexample, the fuel nozzle supply circuits 814 may include a first nozzlecircuit 816, a second nozzle circuit 818, and a third nozzle circuit820. Each of these fuel nozzle supply circuits 814 (e.g., 816, 818, and820) may include one or more fuel lines, oxidant lines, and/or diluentlines (e.g., exhaust lines, steam lines, nitrogen lines, and/or otherinert gas lines), which are fluidly coupled to at least one fuel nozzle164. In the illustrated embodiment, the first nozzle circuit 816 iscoupled to a first set of fuel nozzles 164 (e.g., the central fuelnozzle 790), the second nozzle circuit 818 is coupled to a second set offuel nozzles 164 (e.g., outer fuel nozzles 794, 798, and 802), and thethird nozzle circuit 820 is coupled to a third set of fuel nozzles 164(e.g., outer fuel nozzles 792, 796, and 800). In some embodiments, eachset of fuel nozzles 164 coupled to one of the nozzle supply circuits 814may be entirely diffusion fuel nozzles, entirely premix fuel nozzles, orany combination of diffusion fuel nozzles and premix fuel nozzles.However, any number or configuration of fuel nozzles 164 may be coupledto each fuel nozzle supply circuit 814, and any number of nozzle supplycircuits 814 may be coupled to the fuel nozzles 164. Again, the fuelnozzle supply circuits 814 are coupled to the fluid supply system 518,which may include valves, flow regulators, and other flow controls tocontrol the flow rate and pressure of the flows to the fuel nozzles 164.

In turn, the fluid supply system 518 is coupled to the control system100, which may use the controller 118 to receive the sensor feedback 130and provide controls signals 306 to the fluid supply system 518 tocontrol operation of the circuits 812 and 814. In the illustratedembodiment, the controller 118 of the system 100 may store and execute(e.g., computer instructions or code relating to) a stoichiometriccontrol mode 822 and a non-stoichiometric control mode 824, which mayfurther include a fuel-lean control mode 826 and a fuel-rich controlmode 828. The controller 118 of the system 100 also may store andexecute (e.g., computer instructions or code relating to) a fluid supplycontrol 830, including a first fluid circuit control 832, a second fluidcircuit control 834, and a third fluid circuit control 836. For example,the first fluid circuit control 832 may be configured to control variousflow rates (e.g., oxidant 68, fuel 70, and/or diluent 514) to the firstnozzle circuit 816, the second fluid circuit control 834 may beconfigured to control various flow rates (e.g., oxidant 68, fuel 70,and/or diluent 514) to the second nozzle circuit 818, and the thirdfluid circuit control 836 may be configured to control various flowrates (e.g., oxidant 68, fuel 70, and/or diluent 514) to the thirdnozzle circuit 820.

In certain embodiments, the stoichiometric control mode 822 isconfigured to change the flow rates of at least one fuel 70 and at leastone oxidant 68 and provide a substantially stoichiometric ratio of thefuel 70 with the oxidant 68, whereas the non-stoichiometric control mode824 is configured to change the flow rates and provide anon-stoichiometric ratio of the fuel 70 with the oxidant 68. Forexample, the stoichiometric control mode 822 may be configured toprovide the substantially stoichiometric ratio with an equivalence ratioof approximately 1.0, or between approximately 0.95 and approximately1.05. In contrast, the non-stoichiometric control mode 824 may beconfigured to provide the non-stoichiometric ratio with an equivalenceratio of less than approximately 0.95 or greater than approximately1.05. In some embodiments, the control system 100 may be configured tochange the flow rates from a first set of flow rates to a second set offlow rates, wherein the first and second flow rates are different fromone another (e.g., greater or lesser than one another). The controlledchange in flow rates may also involve a transition between thestoichiometric control mode 822 and the non-stoichiometric control mode824, or the controlled change in flow rates may involve maintaining thesubstantially stoichiometric ratio. The controlled change in flow ratesalso may involve a change in power output (or load) of the SEGR gasturbine system 52 from a first power output (or first load) to a secondpower output (or second load), wherein the first and second poweroutputs (e.g., loads) are different from one another (e.g., lesser orgreater than one another). For example, the controlled change in poweroutputs may involve a controlled change in turbine load, e.g., areduction from a rated or normal load (e.g., 100 percent) to a partialload (e.g., 50 percent). The controlled change in flow rates also mayinvolve maintaining emissions in the exhaust gas within one or moretarget emissions ranges, wherein the emissions may include carbonmonoxide, oxygen, nitrogen oxides, sulfur oxides, unburnt hydrocarbons,hydrogen, or any combination thereof. In certain embodiments, the one ormore target emissions ranges may include an oxygen range of less thanapproximately 50 parts per million by volume (ppmv) and/or a carbonmonoxide range of less than approximately 5000 ppmv. In otherembodiments, the one or more target emissions ranges comprise an oxygenrange of less than approximately 10 ppmv and/or a carbon monoxide rangeof less than approximately 1000 ppmv.

In some embodiments, the control system 100 in the stoichiometriccontrol mode 822 is configured to maintain the substantiallystoichiometric ratio while progressively reducing the flow rates (e.g.,oxidant 68 and fuel 70) among a plurality of sets of flow rates,progressively reducing a power output (e.g., load) of the SEGR gasturbine system 52 among a plurality of power outputs (e.g., full load,first partial load, second partial load, etc.), and maintainingemissions in the exhaust gas within one or more target emissions ranges.The control system 100 also may be configured to transition from thestoichiometric control mode 822 to the non-stoichiometric control mode824 after progressively reducing the flow rates, progressively reducingthe power output, and maintaining emissions. After the transition fromthe stoichiometric control mode 822 to the non-stoichiometric controlmode 824, the control system 100 also may be configured to operate in afuel-rich control mode or a fuel-lean control mode of thenon-stoichiometric control mode 824. The control system 100 also may beconfigured to maintain emissions in the exhaust gas within a first setof target emissions ranges (e.g., while operating in the stoichiometriccontrol mode 822) and a second set of target emissions ranges (e.g.,while operating in the non-stoichiometric control mode 824), wherein thefirst and second sets of target emissions ranges are different from oneanother. Although the foregoing examples provide a number of controlscenarios for the SEGR gas turbine engine 52, it should be understoodthat any number of control scenarios may be executed by the controlsystem 100 using diffusion fuel nozzles, premix fuel nozzles, or anycombination thereof.

FIG. 18 is a graph of exhaust gas recirculation (EGR) flow rate and gasturbine load 840 versus fuel/oxidant ratio 842 for the SEGR gas turbinesystem 52, illustrating a diffusion flame operability curve 844 and apremix flame operability curve 846. The EGR flow rate through the SEGRgas turbine system 52 is generally proportionally to the load on the gasturbine engine 150, and thus the Y-axis 840 generally indicates both EGRflow rate and gas turbine load. In general, the areas above and to theleft of each curve 844 and 846 represent unstable regions for each flameconfiguration of the SEGR gas turbine system 52. It is noteworthy thatthe diffusion flame operability curve 844 substantially exceeds thepremix flame operability curve 846, indicating a substantially greaterEGR flow rate and load range for the SEGR gas turbine system 52operating with diffusion combustion. As illustrated in FIG. 18, thediffusion flame operability curve 844 may correspond to a combustor 160equipped with a diffusion fuel nozzle 554, wherein exhaust gas (e.g.,diluent) is injected downstream from the diffusion fuel nozzle 554 afterthe point of combustion and/or downstream from the diffusion flame 556generated by the nozzle 554. One example of such a diffusion combustionconfiguration is illustrated in FIG. 16. In contrast, the premix flameoperability curve 846 may correspond to a combustor 160 equipped with apremix fuel nozzle 550, wherein the oxidant 68, the fuel 70, and thediluent 514 (e.g., exhaust gas) are premixed prior to the point ofcombustion (i.e., upstream from the premix flame 552). Again, thediffusion flame operability curves 844 indicates much greater EGR flowrates through the SEGR gas turbine system 52, which also means a greaterproduction of CO₂ for use in the target systems 422. The SEGR gasturbine system 52 operating with the foregoing diffusion combustionconfiguration also may have substantially reduced emissions of oxygenand carbon monoxide. These emissions reductions may be at leastpartially due to the independent control of the flows of oxidant 68,fuel 70, and diluent 514 (e.g., exhaust gas). It is believed thatvarious configurations of diffusion fuel nozzles 554 and diluentinjection (e.g., diluent injection system 770 of FIG. 16) maysubstantially increase the operable range of gas turbine loads,throughput of exhaust gas, and output of the exhaust gas 42 (e.g.,streams 95) for use in the target systems 422, such as the hydrocarbonproduction system 12.

ADDITIONAL DESCRIPTION

By way of example, the following clauses are offered as furtherdescription of the present disclosure:

Embodiment 1

A system, comprising: a turbine combustor comprising a first diffusionfuel nozzle, wherein the first diffusion fuel nozzle comprises first andsecond passages that separately inject respective first and second flowsinto a chamber of the turbine combustor to produce a diffusion flame,wherein the first flow comprises a first fuel, and the second flowcomprises a first oxidant and a first diluent; a turbine driven bycombustion products from the diffusion flame in the turbine combustor;and an exhaust gas compressor, wherein the exhaust gas compressor isconfigured to compress and route an exhaust gas from the turbine to theturbine combustor along an exhaust recirculation path.

Embodiment 2

The system of embodiment 1, wherein the first diluent comprises aportion of the exhaust gas, steam, nitrogen, another inert gas, or anycombination thereof.

Embodiment 3

The system of any preceding embodiment, wherein the first diluentcomprises a portion of the exhaust gas.

Embodiment 4

The system of any preceding embodiment, wherein the first diluentcomprises steam.

Embodiment 5

The system of any preceding embodiment, wherein the first diluentcomprises an inert gas.

Embodiment 6

The system of any preceding embodiment, wherein the inert gas comprisesnitrogen.

Embodiment 7

The system of any preceding embodiment, wherein the first and secondpassages have respective first and second outlets that are disposedalong a downstream end of the first diffusion fuel nozzle, and the firstand second passages are isolated from one another along the firstdiffusion fuel nozzle.

Embodiment 8

The system of any preceding embodiment, wherein the first and secondpassages are disposed in a concentric arrangement.

Embodiment 9

The system of any preceding embodiment, wherein the first passageextends around the second passage.

Embodiment 10

The system of any preceding embodiment, wherein the second passageextends around the first passage.

Embodiment 11

The system of any preceding embodiment, wherein the first diffusion fuelnozzle comprises a third passage separate from the first and secondpassages, the third passage is configured to inject a third flow intothe chamber separately from the first and second flows, and the thirdflow comprises a second fuel, a second diluent, or a second oxidant.

Embodiment 12

The system of any preceding embodiment, wherein the third flow comprisesthe second fuel, and the first and second fuels are the same ordifferent from one another.

Embodiment 13

The system of any preceding embodiment, wherein the third flow comprisesthe second oxidant, and the first and second oxidants are the same ordifferent from one another.

Embodiment 14

The system of any preceding embodiment, wherein the third flow comprisesthe second oxidant and the second diluent.

Embodiment 15

The system of any preceding embodiment, wherein the first and secondoxidants are the same as one another, or the first and second diluentsare the same as one another, or a combination thereof.

Embodiment 16

The system of any preceding embodiment, wherein the first and secondoxidants are different from one another, or the first and seconddiluents are different from one another, or a combination thereof.

Embodiment 17

The system of any preceding embodiment, wherein the first and secondoxidants are different from one another and the first and seconddiluents are the same as one another, or the first and second oxidantsare the same as one another and the first and second diluents aredifferent from one another.

Embodiment 18

The system of any preceding embodiment, wherein the first and seconddiluents comprise portions of the exhaust gas.

Embodiment 19

The system of any preceding embodiment, wherein the first diffusion fuelnozzle comprises a fourth passage separate from the first, second, andthird passages, wherein the fourth passage is configured to inject afourth flow into the chamber separately from the first, second, andthird flows, wherein the fourth flow comprises a third fuel, a thirddiluent, or a third oxidant.

Embodiment 20

The system of any preceding embodiment, wherein the turbine combustorcomprises a second diffusion fuel nozzle.

Embodiment 21

The system of any preceding embodiment, wherein the turbine combustorcomprises a first premix fuel nozzle.

Embodiment 22

The system of any preceding embodiment, wherein the turbine combustorcomprises a diluent injection system disposed downstream from the firstdiffusion fuel nozzle.

Embodiment 23

The system of any preceding embodiment, wherein the diluent injectionsystem is configured to inject a portion of the exhaust gas, steam,nitrogen, or another inert gas, or a combination thereof, into thechamber of the turbine combustor downstream from the first diffusionfuel nozzle.

Embodiment 24

The system of any preceding embodiment, wherein the diluent injectionsystem comprises a plurality of openings in a liner of the turbinecombustor, and the plurality of openings is configured to inject theportion of the exhaust gas into the chamber of the turbine combustor.

Embodiment 25

The system of any preceding embodiment, wherein the turbine combustorcomprises a first wall disposed about the chamber, a second walldisposed about the first wall, and an exhaust passage disposed betweenthe first and second walls, wherein the diluent injection systemcomprises a plurality of diluent injectors extending through the firstand second walls of the turbine combustor.

Embodiment 26

The system of any preceding embodiment, wherein the plurality of diluentinjectors is configured inject the portion of the exhaust gas, steam,nitrogen, or another inert gas into the chamber of the turbinecombustor.

Embodiment 27

The system of any preceding embodiment, comprising a first catalyst unitdisposed along the exhaust recirculation path.

Embodiment 28

The system of any preceding embodiment, wherein the first catalyst unitis configured to control concentration levels of carbon monoxide, carbondioxide, and unburnt hydrocarbons in the exhaust gas.

Embodiment 29

The system of any preceding embodiment, wherein the first catalyst unitcomprises an oxidation catalyst, a carbon monoxide catalyst, an aluminumoxide, a zirconium oxide, a silicone oxide, a titanium oxide, a platinumoxide, a palladium oxide, a cobalt oxide, or a mixed metal oxide, or acombination thereof.

Embodiment 30

The system of any preceding embodiment, wherein the oxidation catalystunit is configured to drive an oxidizing reaction with the exhaust gasand an oxidant fuel.

Embodiment 31

The system of any preceding embodiment, comprising a control systemconfigured to adjust a flow of the oxidant fuel to control the oxidizingreaction.

Embodiment 32

The system of any preceding embodiment, wherein the control system isconfigured to adjust the flow of the oxidant fuel in response to sensorfeedback, and the sensor feedback comprises gas composition feedbackindicative of oxygen, carbon monoxide, hydrogen, nitrogen oxides,unburnt hydrocarbons, or any combination thereof.

Embodiment 33

The system of any preceding embodiment, comprising a first heat recoveryunit disposed along the exhaust recirculation path.

Embodiment 34

The system of any preceding embodiment, comprising a catalyst and heatrecovery system having the first catalyst unit and the first heatrecovery unit.

Embodiment 35

The system of any preceding embodiment, wherein the first catalyst unitis disposed upstream, downstream, or integrated with the first heatrecovery unit.

Embodiment 36

The system of any preceding embodiment, comprising a second heatrecovery unit disposed along the exhaust recirculation path.

Embodiment 37

The system of any preceding embodiment, comprising a second catalystunit disposed along the exhaust recirculation path.

Embodiment 38

The system of any preceding embodiment, wherein the first heat recoveryunit comprises a first heat recovery steam generator.

Embodiment 39

The system of any preceding embodiment, comprising a first steam turbinecoupled to the first heat recovery steam generator.

Embodiment 40

The system of any preceding embodiment, wherein the first heat recoveryunit comprises a first heat recovery steam generator and the second heatrecovery unit comprises a second heat recovery steam generator.

Embodiment 41

The system of any preceding embodiment, comprising a first steam turbinecoupled to the first heat recovery steam generator, and a second steamturbine coupled to the second heat recovery steam generator.

Embodiment 42

The system of any preceding embodiment, comprising a moisture removalsystem disposed along the exhaust recirculation path.

Embodiment 43

The system of any preceding embodiment, wherein the moisture removalsystem comprises a heat exchanger, a condenser, a water gas separator, afilter, or any combination thereof.

Embodiment 44

The system of any preceding embodiment, comprising a particulate removalsystem disposed along the exhaust recirculation path.

Embodiment 45

The system of any preceding embodiment, wherein the particulate removalsystem comprises an inertial separator, a gravity separator, a filter,or any combination thereof.

Embodiment 46

The system of any preceding embodiment, comprising a booster blowerdisposed along the exhaust recirculation path.

Embodiment 47

The system of any preceding embodiment, comprising a heat recovery unit,a booster blower, a moisture removal unit, and a particulate removalunit disposed along the exhaust recirculation path.

Embodiment 48

The system of any preceding embodiment, comprising an exhaust gasextraction system configured to extract a portion of the exhaust gas.

Embodiment 49

The system of any preceding embodiment, comprising an exhaust gastreatment system configured to treat the portion of the exhaust gas.

Embodiment 50

The system of any preceding embodiment, wherein the exhaust gastreatment system comprises a gas separation system configured toseparate the portion of the exhaust gas into a plurality of gas streams.

Embodiment 51

The system of any preceding embodiment, wherein the plurality of gasstreams comprises a first stream that is carbon dioxide (CO₂) rich and asecond stream that is carbon dioxide (CO₂) lean.

Embodiment 52

The system of any preceding embodiment, wherein the first stream isnitrogen (N₂) lean and the second stream is nitrogen (N₂) rich.

Embodiment 53

The system of any preceding embodiment, wherein the exhaust gastreatment system comprises a gas compression system, a moisture removalsystem, a particulate removal system, or a combination thereof,configured to receive at least one of the first or second streams.

Embodiment 54

The system of any preceding embodiment, wherein the exhaust gastreatment system comprises a gas purification system configured topurify at least one of the plurality of gas streams.

Embodiment 55

The system of any preceding embodiment, comprising a target systemconfigured to receive at least one of the plurality of streams, whereinthe target system comprises a hydrocarbon production system, asubterranean reservoir, a carbon sequestration system, a pipeline, astorage tank, or any combination thereof.

Embodiment 56

The system of any preceding embodiment, wherein the exhaust gastreatment system comprises a compression system configured to compressthe portion of the exhaust gas.

Embodiment 57

The system of any preceding embodiment, wherein the exhaust gastreatment system comprises a moisture removal system and/or aparticulate removal system.

Embodiment 58

The system of any preceding embodiment, comprising a control systemresponsive to sensor feedback to adjust one or more operating parametersto control an equivalence ratio or emissions levels in the exhaust gas.

Embodiment 59

The system of any preceding embodiment, wherein the one or moreoperating parameters comprise an oxidant flow rate and/or a fuel flowrate to the turbine combustor.

Embodiment 60

The system of any preceding embodiment, wherein the control system isconfigured to maintain the equivalence ratio between approximately 0.95and 1.05.

Embodiment 61

The system of any preceding embodiment, wherein the sensor feedbackcomprises gas composition feedback relating to oxygen, carbon monoxide,hydrogen, nitrogen oxides, unburnt hydrocarbons, or any combinationthereof.

Embodiment 62

The system of any preceding embodiment, wherein the control system iscoupled to a plurality of sensors configured to obtain the sensorfeedback, and the plurality of sensors are disposed along the exhaustrecirculation path, the turbine combustor, the turbine, the exhaust gascompressor, or a combination thereof.

Embodiment 63

The system of any preceding embodiment, comprising a bypass line fromthe exhaust gas compressor to the turbine, wherein the bypass linecomprises a heat exchanger configured to cool a bypass flow of theexhaust gas from the exhaust gas compressor to the turbine.

Embodiment 64

The system of any preceding embodiment, comprising a gas turbine enginehaving the turbine combustor, the turbine, and the exhaust gascompressor, wherein the gas turbine engine is a stoichiometric exhaustgas recirculation (SEGR) gas turbine engine.

Embodiment 65

The system of any preceding embodiment, comprising an exhaust gasextraction system coupled to the gas turbine engine.

Embodiment 66

The system of any preceding embodiment, comprising an exhaust gastreatment system coupled to the exhaust gas extraction system.

Embodiment 67

The system of any preceding embodiment, comprising a hydrocarbonproduction system coupled to the exhaust gas extraction system.

Embodiment 68

A method, comprising: injecting first and second flows separately into achamber of a turbine combustor to produce a diffusion flame, wherein thefirst flow comprises a first fuel, and the second flow comprises a firstoxidant and a first diluent; driving a turbine with combustion productsfrom the diffusion flame, and outputting an exhaust gas; recirculatingthe exhaust gas along an exhaust recirculation path to an exhaust gascompressor; compressing and routing the exhaust gas to the turbinecombustor.

Embodiment 69

The method of any preceding embodiment, wherein the first diluentcomprises a portion of the exhaust gas, steam, nitrogen, another inertgas, or any combination thereof.

Embodiment 70

The method of any preceding embodiment, wherein the first diluentcomprises a portion of the exhaust gas.

Embodiment 71

The method of any preceding embodiment, wherein injecting comprisesseparately injecting the first and second flows from respective firstand second passages that are isolated from one another along a firstdiffusion fuel nozzle.

Embodiment 72

The method of any preceding embodiment, wherein the first and secondpassages are disposed in a concentric arrangement.

Embodiment 73

The method of any preceding embodiment, wherein the first passageextends around the second passage.

Embodiment 74

The method of any preceding embodiment, wherein the second passageextends around the first passage.

Embodiment 75

The method of any preceding embodiment, wherein injecting comprisesseparately injecting the first flow, the second flow, and a third flowfrom respective first, second, and third passages that are isolated fromone another along a first diffusion fuel nozzle, wherein the third flowcomprises a second fuel, a second diluent, or a second oxidant.

Embodiment 76

The method of any preceding embodiment, wherein the third flow comprisesthe second fuel, and the first and second fuels are the same ordifferent from one another.

Embodiment 77

The method of any preceding embodiment, wherein the third flow comprisesthe second oxidant, and the first and second oxidants are the same ordifferent from one another.

Embodiment 78

The method of any preceding embodiment, wherein the third flow comprisesthe second oxidant and the second diluent.

Embodiment 79

The method of any preceding embodiment, wherein the first and secondoxidants are the same as one another, or the first and second diluentsare the same as one another, or a combination thereof.

Embodiment 80

The method of any preceding embodiment, wherein the first and secondoxidants are different from one another, or the first and seconddiluents are different from one another, or a combination thereof.

Embodiment 81

The method of any preceding embodiment, wherein the first and secondoxidants are different from one another and the first and seconddiluents are the same as one another, or the first and second oxidantsare the same as one another and the first and second diluents aredifferent from one another.

Embodiment 82

The method of any preceding embodiment, wherein the first and seconddiluents comprise portions of the exhaust gas.

Embodiment 83

The method of any preceding embodiment, wherein injecting comprisesseparately injecting the first flow, the second flow, a third flow, anda fourth flow from respective first, second, third, and fourth passagesthat are isolated from one another along a first diffusion fuel nozzle,wherein the third flow comprises a second fuel, a second diluent, or asecond oxidant, wherein the fourth flow comprises a third fuel, a thirddiluent, or a third oxidant.

Embodiment 84

The method of any preceding embodiment, comprising injecting a diluentflow into the chamber downstream from the first diffusion fuel nozzle.

Embodiment 85

The method of any preceding embodiment, comprising injecting the diluentflow through a plurality of openings in a liner of the turbinecombustor, and the diluent flow comprises a portion of the exhaust gas.

Embodiment 86

The method of any preceding embodiment, comprising injecting the diluentflow through a plurality of diluent injectors extending through at leastone wall of the turbine combustor, and the diluent flow comprises aportion of the exhaust gas, steam, nitrogen, or another inert gas.

Embodiment 87

The method of any preceding embodiment, comprising treating the exhaustgas with a first catalyst unit along the exhaust recirculation path; and

Embodiment 88

The method of any preceding embodiment, wherein treating comprisescontrolling concentration levels of carbon monoxide, carbon dioxide, andunburnt hydrocarbons in the exhaust gas.

Embodiment 89

The method of any preceding embodiment, wherein treating comprisesdriving an oxidizing reaction with the exhaust gas and an oxidant fuel.

Embodiment 90

The method of any preceding embodiment, comprising controlling a flow ofthe oxidant fuel to the first catalyst unit to control the oxidizingreaction.

Embodiment 91

The method of any preceding embodiment, comprising controlling the flowof the oxidant fuel in response to sensor feedback, and the sensorfeedback comprises gas composition feedback indicative of oxygen, carbonmonoxide, hydrogen, nitrogen oxides, unburnt hydrocarbons, or anycombination thereof.

Embodiment 92

The method of any preceding embodiment, comprising recovering heat fromthe exhaust gas along the exhaust recirculation path using a first heatrecovery unit, a second heat recovery unit, or a combination thereof.

Embodiment 93

The method of any preceding embodiment, comprising driving a firstcatalytic reaction with a first catalyst unit within, upstream, ordownstream of the first or second heat recovery unit.

Embodiment 94

The method of any preceding embodiment, comprising driving a secondcatalytic reaction with a second catalyst unit within, upstream, ordownstream of the first or second heat recovery unit.

Embodiment 95

The method of any preceding embodiment, comprising generating a firststeam with a first heat recovery steam generator of the first heatrecovery unit, generating a second steam with a second heat recoverysteam generator of the second heat recovery unit, or a combinationthereof.

Embodiment 96

The method of any preceding embodiment, comprising driving a first steamturbine with the first steam or driving a second steam turbine with thesecond steam.

Embodiment 97

The method of any preceding embodiment, comprising removing moisturefrom the exhaust gas with a moisture removal system disposed along theexhaust recirculation path, or removing particulate from the exhaust gaswith a particulate removal system disposed along the exhaustrecirculation path, or a combination thereof.

Embodiment 98

The method of any preceding embodiment, wherein the moisture removalsystem comprises a heat exchanger, a condenser, a water gas separator, afirst filter, or any combination thereof, wherein the particulateremoval system comprises an inertial separator, a gravity separator, asecond filter, or any combination thereof.

Embodiment 99

The method of any preceding embodiment, comprising boosting a flow ofthe exhaust gas with a booster blower disposed along the exhaustrecirculation path.

Embodiment 100

The method of any preceding embodiment, comprising treating the exhaustgas with a heat recovery unit, a catalyst unit, a booster blower, amoisture removal unit, and a particulate removal unit disposed along theexhaust recirculation path.

Embodiment 101

The method of any preceding embodiment, comprising extracting a portionof the exhaust gas with an exhaust gas extraction system.

Embodiment 102

The method of any preceding embodiment, comprising treating the portionof the exhaust gas with an exhaust gas treatment system.

Embodiment 103

The method of any preceding embodiment, wherein treating the portion ofthe exhaust gas comprises separating the portion of the exhaust gas intoa plurality of gas streams.

Embodiment 104

The method of any preceding embodiment, wherein the plurality of gasstreams comprises a first stream that is carbon dioxide (CO₂) rich and asecond stream that is carbon dioxide (CO₂) lean.

Embodiment 105

The method of any preceding embodiment, wherein treating the portion ofthe exhaust gas comprises compressing the portion of the exhaust gas,the first stream, or the second steam with a gas compression system.

Embodiment 106

The method of any preceding embodiment, wherein treating the portion ofthe exhaust gas comprises removing moisture from the portion of theexhaust gas, the first stream, or the second steam with a moistureremoval system.

Embodiment 107

The method of any preceding embodiment, wherein treating the portion ofthe exhaust gas comprises removing particulate from the portion of theexhaust gas, the first stream, or the second steam with a particulateremoval system.

Embodiment 108

The method of any preceding embodiment, comprising routing the portionof the exhaust gas, the first stream, or the second steam to a targetsystem, wherein the target system comprises a hydrocarbon productionsystem, a subterranean reservoir, a carbon sequestration system, apipeline, a storage tank, or any combination thereof.

Embodiment 109

The method of any preceding embodiment, comprising adjusting one or moreoperating parameters in response to sensor feedback to control anequivalence ratio or emissions levels in the exhaust gas.

Embodiment 110

The method of any preceding embodiment, wherein adjusting the one ormore operating parameters comprises controlling an oxidant flow rateand/or a fuel flow rate to the turbine combustor.

Embodiment 111

The method of any preceding embodiment, wherein adjusting the one ormore operating parameters comprises maintaining the equivalence ratiobetween approximately 0.95 and 1.05.

Embodiment 112

The method of any preceding embodiment, comprising obtaining the sensorfeedback by monitoring a gas composition of the exhaust gas relating tooxygen, carbon monoxide, hydrogen, nitrogen oxides, unburnthydrocarbons, or any combination thereof.

Embodiment 113

The method of any preceding embodiment, wherein obtaining the sensorfeedback comprises monitoring a plurality of sensors disposed along theexhaust recirculation path, the turbine combustor, the turbine, theexhaust gas compressor, or a combination thereof.

Embodiment 114

The method of any preceding embodiment, comprising routing a bypass flowof the exhaust gas along a bypass line from the exhaust gas compressorto the turbine.

Embodiment 115

The method of any preceding embodiment, comprising cooling the bypassflow of the exhaust gas along the bypass line, and cooling the turbineusing the bypass flow of the exhaust gas.

Embodiment 116

The method of any preceding embodiment, comprising operating a gasturbine engine having the turbine combustor, the turbine, and theexhaust gas compressor to achieve substantially stoichiometriccombustion based on sensor feedback.

Embodiment 117

The method of any preceding embodiment, comprising extracting a portionof the exhaust gas with an exhaust gas extraction system coupled to thegas turbine engine, and routing the portion of the exhaust gas to ahydrocarbon production system, a carbon sequestration system, apipeline, a storage tank, or any combination thereof.

Embodiment 118

A method, comprising: introducing an oxidant to at least one oxidantcompressor to produce a compressed oxidant stream; introducing arecirculated low oxygen content gas stream to a compressor section of agas turbine engine to produce a compressed low oxygen content gasstream; mixing a first portion of the compressed low oxygen content gasstream with a first portion of the compressed oxidant stream andproducing a diluted compressed oxidant stream; introducing the dilutedcompressed oxidant stream and a fuel stream in a substantiallystoichiometric ratio to at least one turbine combustor and mixing thediluted compressed oxidant stream and the fuel stream at the point ofcombustion and combusting the mixture of the diluted compressed oxidantstream and the fuel stream; introducing a second portion of thecompressed low oxygen content gas stream to the at least one turbinecombustor and mixing it with the combusting streams of dilutedcompressed oxidant and fuel after the point of combustion and producinga high temperature high pressure low oxygen content stream; introducingthe high temperature high pressure low oxygen content stream to anexpander section of the gas turbine engine and expanding the hightemperature high pressure low oxygen content stream to producemechanical power and a recirculated low oxygen content gas stream; usinga first portion of the mechanical power to drive the compressor sectionof the gas turbine engine; using a second portion of the mechanicalpower to drive at least one of: a generator, the at least one oxidantcompressor or at least one other mechanical device; recirculating therecirculated low oxygen content gas stream in a recirculation loop fromthe outlet of the expander section to the inlet of the compressorsection of the gas turbine engine; and extracting at least a thirdportion of the compressed low oxygen content gas stream from the gasturbine engine and delivering the at least a third portion of thecompressed low oxygen content gas stream to the first at least oneoxidation catalyst unit and producing a low oxygen content productstream.

Embodiment 119

The method of any preceding embodiment, comprising introducing a secondportion of the compressed oxidant stream to the first at least oneoxidation catalyst unit to oxidize at least a portion of the at leastone of carbon monoxide, hydrogen, unburned hydrocarbons or similarproducts of incomplete combustion contained in the third portion of thecompressed low oxygen content gas stream.

Embodiment 120

The method of any preceding embodiment, comprising introducing anoxidation fuel to the first at least one oxidation catalyst unit andreducing at least a portion of the residual oxygen contained in thethird portion of the compressed low oxygen content gas stream.

Embodiment 121

The method of any preceding embodiment, wherein the oxidant consists ofessentially ambient air and the recirculated low oxygen content gasstream comprising comprises nitrogen.

Embodiment 122

The method of any preceding embodiment, wherein the equivalence ratio(phi, φ) is equal to (mol % fuel/mol % oxidant)actual/(mol % fuel/mol %oxidant)stoichiometric.

Embodiment 123

The method of any preceding embodiment, comprising controlling the flowrate of at least one of the first portion of the compressed oxidantstream and the fuel stream to achieve a combustion equivalence ratio ofabout 1 and producing a substantially stoichiometric ratio of the firstportion of the compressed oxidant stream and the fuel stream.

Embodiment 124

The method of any preceding embodiment, comprising sensors installed inthe recirculation loop and measuring the constituents within therecirculated low oxygen content stream.

Embodiment 125

The method of any preceding embodiment, wherein the measuredconstituents are at least one of: oxygen, carbon monoxide, hydrogen,nitrogen oxides, and unburned hydrocarbons.

Embodiment 126

The method of any preceding embodiment, comprising determining theequivalence ratio by analyzing the constituent measurements.

Embodiment 127

The method of any preceding embodiment, comprising at least one sensorinstalled and measuring the constituents within the extracted thirdportion of the compressed low oxygen content gas stream upstream of thefirst at least one oxidation catalyst unit, downstream of the first atleast one oxidation catalyst unit or both.

Embodiment 128

The method of any preceding embodiment, wherein the measuredconstituents are at least one of: oxygen, carbon monoxide, hydrogen,nitrogen oxides, and unburned hydrocarbons.

Embodiment 129

The method of any preceding embodiment, comprising at least onecontroller adjusting at least one of the combustion equivalence ratio,the flow rate of the second portion of the compressed oxidant stream orthe flow rate of the oxidation fuel and achieving a desired level of atleast one of the measured constituents downstream of the first at leastone oxidation catalyst unit.

Embodiment 130

The method of any preceding embodiment, comprising a first heat recoveryunit downstream of the first at least one oxidation catalyst unit.

Embodiment 131

The method of any preceding embodiment, wherein the first heat recoveryunit comprises a steam generator.

Embodiment 132

The method of any preceding embodiment, comprising producing steam bythe steam generator that is delivered to at least one steam turbine anddriving at least one of a generator to produce electrical power oranother mechanical device.

Embodiment 133

The method of any preceding embodiment, comprising a second heatrecovery unit in the recirculation loop between the outlet of theexpander section and the inlet to the compressor section of the gasturbine engine and removing heat from the recirculated low oxygencontent gas stream.

Embodiment 134

The method of any preceding embodiment, wherein the second heat recoveryunit comprises a steam generator.

Embodiment 135

The method of any preceding embodiment, comprising producing steam bythe steam generator that is delivered to at least one steam turbine anddriving at least one of a generator to produce electrical power oranother mechanical device.

Embodiment 136

The method of any preceding embodiment, comprising a secondary flow pathdelivering a fourth portion of the compressed low oxygen content gasstream from the compressor section of the gas turbine engine to theturbine as a secondary flow and after cooling and sealing the turbinedelivering the fourth portion of the compressed low oxygen content gasstream into the recirculation loop.

Embodiment 137

The method of any preceding embodiment, comprising a booster blower inthe recirculation loop increasing the pressure of the recirculated lowoxygen content gas stream downstream of the second heat recovery unit.

Embodiment 138

The method of any preceding embodiment, comprising a heat exchangerwithin the recirculation loop upstream of the compressor section of thegas turbine engine cooling the recirculated low oxygen content gasstream before entering the inlet of the compressor section of the gasturbine engine.

Embodiment 139

The method of any preceding embodiment, comprising condensing andremoving water from the recirculated low oxygen content gas stream withthe heat exchanger.

Embodiment 140

The method of any preceding embodiment, comprising delivering at least aportion of the low oxygen content product stream to a subterraneanreservoir for enhanced hydrocarbon recovery.

Embodiment 141

The method of any preceding embodiment, comprising compressing the atleast a portion of the low oxygen content product stream with at leastone inert gas product compressor prior to delivering the at least aportion of the low oxygen content product stream to a subterraneanreservoir for enhanced hydrocarbon recovery.

Embodiment 142

The method of any preceding embodiment, comprising cooling the lowoxygen content product stream by the first heat recovery unit.

Embodiment 143

The method of any preceding embodiment, comprising delivering the atleast a portion of the low oxygen content product stream to a gasdehydration unit.

Embodiment 144

The method of any preceding embodiment, comprising delivering at least aportion of the low oxygen content product stream to a carbon dioxideseparation unit to produce a lean carbon dioxide stream and a richcarbon dioxide stream.

Embodiment 145

The method of any preceding embodiment, comprising delivering at least aportion of the lean carbon dioxide stream to a subterranean reservoirfor enhanced hydrocarbon recovery.

Embodiment 146

The method of any preceding embodiment, comprising delivering at least aportion of the rich carbon dioxide stream to a subterranean reservoirfor enhanced hydrocarbon recovery.

Embodiment 147

The method of any preceding embodiment, comprising delivering at least aportion of the rich carbon dioxide stream to a carbon sequestrationunit.

Embodiment 148

The method of any preceding embodiment, comprising compressing the atleast a portion of the lean carbon dioxide stream to at least one leanproduct compressor prior to delivering the lean carbon dioxide stream toa subterranean reservoir for enhanced hydrocarbon recovery.

Embodiment 149

The method of any preceding embodiment, comprising compressing the atleast a portion of the rich carbon dioxide stream to at least one richproduct compressor prior to delivering the rich carbon dioxide stream toa subterranean reservoir for enhanced hydrocarbon recovery.

Embodiment 150

The method of any preceding embodiment, comprising compressing the atleast a portion of the rich carbon dioxide stream to at least one richproduct compressor prior to delivering the rich carbon dioxide stream toa carbon sequestration unit.

Embodiment 151

The method of any preceding embodiment, comprising delivering at least aportion of the lean carbon dioxide stream to a gas dehydration unit.

Embodiment 152

The method of any preceding embodiment, comprising delivering at least aportion of the rich carbon dioxide stream to a gas dehydration unit.

Embodiment 153

The method of any preceding embodiment, comprising introducing at leasta portion of the low oxygen content product stream to an expander andexpanding the at least a portion of the low oxygen content productstream, driving at least one of a generator or another mechanical deviceand producing a vent stream.

Embodiment 154

The method of any preceding embodiment, comprising introducing at leasta portion of the lean carbon dioxide stream to an expander and expandingthe at least a portion of the lean carbon dioxide stream, driving atleast one of a generator or another mechanical device and producing avent stream.

Embodiment 155

The method of any preceding embodiment, comprising a second at least oneoxidation catalyst unit located within the recirculation loop andoxidizing at least a portion of the at least one of carbon monoxide,hydrogen, unburned hydrocarbons or similar products of incompletecombustion contained in the recirculated low oxygen content gas stream.

Embodiment 156

The method of any preceding embodiment, wherein the second at least oneoxidation catalyst unit is located upstream of the second heat recoveryunit.

Embodiment 157

The method of any preceding embodiment, wherein the second at least oneoxidation catalyst unit is located downstream of the second heatrecovery unit.

Embodiment 158

The method of any preceding embodiment, wherein the second at least oneoxidation catalyst unit is located within the second heat recovery unitat a location providing a suitable operating temperature and providing asuitable heat sink for the heat generated by the catalytic reactions.

Embodiment 159

The method of any preceding embodiment, comprising controlling the flowrate of the at least a second portion of the compressed low oxygencontent gas stream.

Embodiment 160

The method of any preceding embodiment, wherein the flow rate of the atleast a second portion of the compressed low oxygen content gas streamis adjusted to maintain the pressure at a location within therecirculation loop within a desired range.

Embodiment 161

The method of any preceding embodiment, wherein the flow rate of the atleast a second portion of the compressed low oxygen content gas streamis adjusted by means of at least one of an extraction valve, extractionvent valve, product compressor operating speed, product compressor inletguide vane position or product compressor recycle valve.

Embodiment 162

The method of any preceding embodiment, comprising at least one of aninertial separator, coalescing filter and a water impermeable filterdownstream of the heat exchanger and improving the effectiveness ofremoving the condensed water.

This written description uses examples to disclose the invention,including the best mode, and also to enable any person skilled in theart to practice the invention, including making and using any devices orsystems and performing any incorporated methods. The patentable scope ofthe invention is defined by the claims, and may include other examplesthat occur to those skilled in the art. Such other examples are intendedto be within the scope of the claims if they have structural elementsthat do not differ from the literal language of the claims, or if theyinclude equivalent structural elements with insubstantial differencesfrom the literal language of the claims.

1-162. (canceled)
 163. A system, comprising: a turbine combustorcomprising a first diffusion fuel nozzle, wherein the first diffusionfuel nozzle comprises first and second passages that separately injectrespective first and second flows into a chamber of the turbinecombustor to produce a diffusion flame, wherein the first flow comprisesa first fuel, and the second flow comprises a first oxidant and a firstdiluent; a turbine driven by combustion products from the diffusionflame in the turbine combustor; and an exhaust gas compressor, whereinthe exhaust gas compressor is configured to compress and route anexhaust gas from the turbine to the turbine combustor along an exhaustrecirculation path.
 164. The system of claim 163, wherein the firstdiluent comprises a portion of the exhaust gas, steam, nitrogen, anotherinert gas, or any combination thereof.
 165. The system of claim 163,wherein the first and second passages have respective first and secondoutlets that are disposed along a downstream end of the first diffusionfuel nozzle, and the first and second passages are isolated from oneanother along the first diffusion fuel nozzle.
 166. The system of claim163, wherein the first and second passages are disposed in a concentricarrangement.
 167. The system of claim 163, wherein the first passageextends around the second passage.
 168. The system of claim 163, whereinthe second passage extends around the first passage.
 169. The system ofclaim 163, wherein the first diffusion fuel nozzle comprises a thirdpassage separate from the first and second passages, the third passageis configured to inject a third flow into the chamber separately fromthe first and second flows, and the third flow comprises a second fuel,a second diluent, or a second oxidant.
 170. The system of claim 169,wherein the first diffusion fuel nozzle comprises a fourth passageseparate from the first, second, and third passages, wherein the fourthpassage is configured to inject a fourth flow into the chamberseparately from the first, second, and third flows, wherein the fourthflow comprises a third fuel, a third diluent, or a third oxidant. 171.The system of claim 163, wherein the turbine combustor comprises adiluent injection system disposed downstream from the first diffusionfuel nozzle and configured to inject a portion of the exhaust gas,steam, nitrogen, or another inert gas, or a combination thereof, intothe chamber of the turbine combustor downstream from the first diffusionfuel nozzle.
 172. The system of claim 163, comprising a control systemresponsive to sensor feedback to adjust one or more operating parametersto control an equivalence ratio or emissions levels in the exhaust gas,wherein the one or more operating parameters comprise an oxidant flowrate and/or a fuel flow rate to the turbine combustor, and wherein thecontrol system is configured to maintain the equivalence ratio betweenapproximately 0.95 and 1.05.
 173. A method, comprising: injecting firstand second flows separately into a chamber of a turbine combustor toproduce a diffusion flame, wherein the first flow comprises a firstfuel, and the second flow comprises a first oxidant and a first diluent;driving a turbine with combustion products from the diffusion flame, andoutputting an exhaust gas; recirculating the exhaust gas along anexhaust recirculation path to an exhaust gas compressor; compressing androuting the exhaust gas to the turbine combustor.
 174. The method ofclaim 173, wherein the first diluent comprises a portion of the exhaustgas, steam, nitrogen, another inert gas, or any combination thereof.175. The method of claim 173, wherein injecting comprises separatelyinjecting the first and second flows from respective first and secondpassages that are isolated from one another along a first diffusion fuelnozzle.
 176. The method of claim 173, wherein injecting comprisesseparately injecting the first flow, the second flow, and a third flowfrom respective first, second, and third passages that are isolated fromone another along a first diffusion fuel nozzle, wherein the third flowcomprises a second fuel, a second diluent, or a second oxidant.
 177. Themethod of claim 173, wherein injecting comprises separately injectingthe first flow, the second flow, a third flow, and a fourth flow fromrespective first, second, third, and fourth passages that are isolatedfrom one another along a first diffusion fuel nozzle, wherein the thirdflow comprises a second fuel, a second diluent, or a second oxidant,wherein the fourth flow comprises a third fuel, a third diluent, or athird oxidant.
 178. The method of claim 173, comprising injecting adiluent flow into the chamber downstream from the first diffusion fuelnozzle.
 179. The method of claim 16, comprising injecting the diluentflow through a plurality of openings in a liner of the turbinecombustor, and the diluent flow comprises a portion of the exhaust gas.180. The method of claim 16, comprising injecting the diluent flowthrough a plurality of diluent injectors extending through at least onewall of the turbine combustor, and the diluent flow comprises a portionof the exhaust gas, steam, nitrogen, or another inert gas.
 181. Themethod of claim 173, comprising treating the exhaust gas with a firstcatalyst unit along the exhaust recirculation path, wherein treatingcomprises controlling concentration levels of carbon monoxide, carbondioxide, and unburnt hydrocarbons in the exhaust gas.
 182. The method ofclaim 173, comprising adjusting one or more operating parameters inresponse to sensor feedback to control an equivalence ratio or emissionslevels in the exhaust gas, wherein adjusting the one or more operatingparameters comprises maintaining the equivalence ratio betweenapproximately 0.95 and 1.05.
 183. A method, comprising: introducing anoxidant to at least one oxidant compressor to produce a compressedoxidant stream; introducing a recirculated low oxygen content gas streamto a compressor section of a gas turbine engine to produce a compressedlow oxygen content gas stream; mixing a first portion of the compressedlow oxygen content gas stream with a first portion of the compressedoxidant stream and producing a diluted compressed oxidant stream;introducing the diluted compressed oxidant stream and a fuel stream in asubstantially stoichiometric ratio to at least one turbine combustor andmixing the diluted compressed oxidant stream and the fuel stream at thepoint of combustion and combusting the mixture of the diluted compressedoxidant stream and the fuel stream; introducing a second portion of thecompressed low oxygen content gas stream to the at least one turbinecombustor and mixing it with the combusting streams of dilutedcompressed oxidant and fuel after the point of combustion and producinga high temperature high pressure low oxygen content stream; introducingthe high temperature high pressure low oxygen content stream to anexpander section of the gas turbine engine and expanding the hightemperature high pressure low oxygen content stream to producemechanical power and a recirculated low oxygen content gas stream; usinga first portion of the mechanical power to drive the compressor sectionof the gas turbine engine; using a second portion of the mechanicalpower to drive at least one of: a generator, the at least one oxidantcompressor or at least one other mechanical device; recirculating therecirculated low oxygen content gas stream in a recirculation loop fromthe outlet of the expander section to the inlet of the compressorsection of the gas turbine engine; and extracting at least a thirdportion of the compressed low oxygen content gas stream from the gasturbine engine and delivering the at least a third portion of thecompressed low oxygen content gas stream to the first at least oneoxidation catalyst unit and producing a low oxygen content productstream.
 184. The method of claim 183, comprising introducing a secondportion of the compressed oxidant stream to the first at least oneoxidation catalyst unit to oxidize at least a portion of the at leastone of carbon monoxide, hydrogen, unburned hydrocarbons or similarproducts of incomplete combustion contained in the third portion of thecompressed low oxygen content gas stream.
 185. The method of claim 183,comprising introducing an oxidation fuel to the first at least oneoxidation catalyst unit and reducing at least a portion of the residualoxygen contained in the third portion of the compressed low oxygencontent gas stream.
 186. The method of claim 183, comprising: measuringthe constituents within the extracted third portion of the compressedlow oxygen content gas stream upstream of the first at least oneoxidation catalyst unit, downstream of the first at least one oxidationcatalyst unit or both, wherein the measured constituents are at leastone of: oxygen, carbon monoxide, hydrogen, nitrogen oxides, or unburnedhydrocarbons; adjusting at least one of the combustion equivalenceratio, the flow rate of the second portion of the compressed oxidantstream or the flow rate of the oxidation fuel; and achieving a desiredlevel of at least one of the measured constituents downstream of thefirst at least one oxidation catalyst unit.
 187. The method of claim183, comprising delivering at least a portion of the low oxygen contentproduct stream to a subterranean reservoir for enhanced hydrocarbonrecovery.